CN116293742A - Device and process method for incinerating waste gas and waste liquid in process of preparing ethylene glycol from coal - Google Patents
Device and process method for incinerating waste gas and waste liquid in process of preparing ethylene glycol from coal Download PDFInfo
- Publication number
- CN116293742A CN116293742A CN202310230945.1A CN202310230945A CN116293742A CN 116293742 A CN116293742 A CN 116293742A CN 202310230945 A CN202310230945 A CN 202310230945A CN 116293742 A CN116293742 A CN 116293742A
- Authority
- CN
- China
- Prior art keywords
- gas
- waste liquid
- waste
- incinerator
- combustion
- 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.)
- Pending
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 110
- 239000002699 waste material Substances 0.000 title claims abstract description 107
- 239000002912 waste gas Substances 0.000 title claims abstract description 76
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 75
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 34
- 239000003245 coal Substances 0.000 title claims description 19
- 239000007789 gas Substances 0.000 claims abstract description 86
- 239000001301 oxygen Substances 0.000 claims abstract description 79
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 79
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 78
- 239000000779 smoke Substances 0.000 claims abstract description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 85
- 239000003546 flue gas Substances 0.000 claims description 84
- 238000011084 recovery Methods 0.000 claims description 43
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 42
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 39
- 238000005406 washing Methods 0.000 claims description 35
- 238000002485 combustion reaction Methods 0.000 claims description 34
- 239000000446 fuel Substances 0.000 claims description 23
- 239000003345 natural gas Substances 0.000 claims description 19
- 239000007921 spray Substances 0.000 claims description 18
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical class O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 13
- 230000008929 regeneration Effects 0.000 claims description 11
- 238000011069 regeneration method Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 7
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 claims description 6
- 238000005336 cracking Methods 0.000 claims description 6
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 10
- 239000002737 fuel gas Substances 0.000 abstract description 10
- 231100000719 pollutant Toxicity 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 2
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 description 60
- BLLFVUPNHCTMSV-UHFFFAOYSA-N methyl nitrite Chemical compound CON=O BLLFVUPNHCTMSV-UHFFFAOYSA-N 0.000 description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 12
- 239000000126 substance Substances 0.000 description 11
- 230000001105 regulatory effect Effects 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 8
- 229920006395 saturated elastomer Polymers 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 238000004880 explosion Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000006378 damage Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- NKDDWNXOKDWJAK-UHFFFAOYSA-N dimethoxymethane Chemical compound COCOC NKDDWNXOKDWJAK-UHFFFAOYSA-N 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000035945 sensitivity Effects 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000002528 anti-freeze Effects 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000002146 bilateral effect Effects 0.000 description 1
- 230000008033 biological extinction Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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
-
- 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
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- 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
- F23L5/00—Blast-producing apparatus before the fire
- F23L5/02—Arrangements of fans or blowers
-
- 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
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
Abstract
The invention belongs to the technical field of waste gas and waste liquid incineration, in particular to a device and a process method for waste gas and waste liquid incineration in a coal-to-ethylene glycol process, comprising a circulating blower device, an oxygen supply system and a combustion-supporting gas mixer; according to the requirements of the emission standard of atmospheric pollutants of a thermal power plant GB13223-2011 and the comprehensive emission standard of atmospheric pollutants GB 16297-1996, the invention greatly reduces the smoke discharged into the atmosphere, thereby reducing the emission of NOx and effectively protecting the environment; compared with air as fuel gas, the invention has the advantages of less cold energy consumption, high utilization rate of burning heat, less loss, low investment cost, less thermal NOx and rapid NOx generation, etc.
Description
Technical Field
The invention belongs to the technical field of waste gas and waste liquid treatment, and particularly relates to a device and a process method for incinerating waste gas and waste liquid in a coal-to-ethylene glycol process.
Background
Ethylene glycol is an important organic chemical raw material, is mainly used for producing polyester series products and automobile antifreeze, can be used as a surfactant, a deicing agent and a chemical intermediate product, and has wide application in the chemical industry due to the active chemical property of the ethylene glycol with double hydroxyl groups. The process for preparing ethylene glycol from coal is characterized by taking coal as a raw material and can be divided into three types according to different process flows: the direct process, the oxalate process and the olefin process, however, no matter which process technology is adopted, the coal is gasified, transformed and purified to prepare the synthetic gas, and finally the ethylene glycol is generated. The three process routes of the coal-to-ethylene glycol all generate waste in the production processThe waste gas mainly comprises PSA tail gas, methanol rectification tail gas, MN regeneration tower tail gas of DMO section, waste liquid mainly comprises MF waste liquid at the top of MF separation tower of DMO rectification section and MF light fraction waste liquid at the top of light tower of DMC recovery section, and the waste gas and waste liquid contain hydrogen, carbon monoxide, methane, MN (methyl nitrite), MF (methyl formate), ML (dimethoxy methane), ME (methanol), DMC (dimethyl carbonate) and oxynitride (NO) X ) Among various harmful substances in substances such as DMC (dimethyl carbonate), NOx is one of main pollution sources causing atmospheric pollution, and can cause damages such as photochemical smog, acid rain, ozone layer cavity and the like, methyl Nitrite (MN) and alcohol esters can not be directly discharged, and the environment is polluted after the waste is discharged.
For a large amount of waste gas and waste liquid produced by a large-scale glycol production device, because the sources of the components are different and dispersed, the components are complex, the heat value is different, the device also has the characteristics of inflammability, explosiveness, easy corrosion, easy decomposition and the like, the prior art is to send the waste gas and waste liquid into an incinerator to be mixed with air for combustion, however, the volume content of oxygen in the air is 20.95 percent, and N 2 Is 78.09% by volume, so that there is a large amount of N during combustion 2 Is sent to the incinerator, although N 2 Does not participate in combustion reaction in the combustion furnace, but is large in N 2 The concentration of NOx is diluted. According to the requirements of the emission standard of atmospheric pollutants of a thermal power plant GB13223-2011 and the comprehensive emission standard of atmospheric pollutants GB 16297-1996, although NOx in the discharged flue gas meets the emission requirements, the total amount of NOx discharged can be caused by N 2 Is fed to the incinerator for dilution and more, so that the total amount of NOx discharged to the atmosphere is more. On the other hand, the air needs to be preheated from room temperature to 160-250 ℃ before being sent into the incinerator, a large amount of heat sources need to be consumed, the room temperature is lower in winter, and the heat sources consume more; and when the smoke is discharged, the temperature is about 140 ℃, and a large amount of smoke takes away part of heat, so that the resource waste of a heat source is caused.
Disclosure of Invention
Based on the prior art, the invention provides a device and a process method for incinerating waste gas and waste liquid in a coal-to-ethylene glycol process, and the device and the method have the advantages of low NOx emission, low cold energy consumption, high incineration heat utilization rate, low loss, low investment cost, low thermal NOx and rapid NOx generation amount and the like.
In order to solve the technical problems, the technical scheme of the invention is as follows:
the device for incinerating waste gas and waste liquid in the process of preparing ethylene glycol from coal comprises an incinerator, a fuel supply system, an SCR (selective catalytic reduction) reactor, a washing device, a circulating blower device and an oxygen supply system; the incinerator is used for incinerating waste gas and waste liquid generated in the coal-to-ethylene glycol; the fuel inlet of the incinerator is connected with the fuel supply system through a pipeline; the SCR reactor is used for catalyzing and reducing nitrogen oxide compounds in the flue gas into N 2 And H 2 O, simultaneously catalytically cracking dioxin in flue gas into CO 2 、H 2 O and HCl; the combustion-supporting gas inlet of the incinerator is connected to the outlet of the circulating blower device through a pipeline and a combustion-supporting gas mixer, and the combustion-supporting gas mixer is also connected to an oxygen supply system through a pipeline; the combustion-supporting gas mixer is used for uniformly mixing the circulating smoke and oxygen; the flue gas outlet of the incinerator is connected to the inlet of the SCR reactor through a flue; the flue gas outlet of the SCR reactor is respectively connected to the inlet of the circulating blower device and the inlet of the washing device in two paths through a flue.
Further, a flue with a flue gas outlet of the incinerator connected with an inlet of the SCR reactor is also provided with a heat recovery device; the heat recovery device is used for recovering heat of flue gas generated in the incinerator; and the pipeline connected with the combustion-supporting gas mixer of the incinerator and the pipeline connected with the outlet of the circulating blower device of the combustion-supporting gas mixer are both provided with an online oxygen analyzer.
Further, the circulating blower device is formed by connecting a plurality of blowers in parallel, and each blower is provided with an air inlet.
Further, the heat recovery device comprises a high-temperature heat recovery device and a low-temperature heat recovery device; the low-temperature heat recovery device is a superheater, and the low-temperature heat recovery device is a boiler; and an SNCR device is arranged in the high-temperature heat recovery device.
Further, the fuel supply system comprises a natural gas supply system, an exhaust gas supply system and a waste liquid supply system, and bypass pipelines for removing the torch are arranged.
Further, the natural gas supply system, the waste gas supply system and the waste liquid supply system are all independently provided with pipelines and are communicated with the spray gun in the incinerator; the oxygen supply system is provided with a standby oxygen supply system.
A waste gas and waste liquid incineration process method in a coal glycol process comprises the following steps:
waste gas and waste liquid generated in the ethylene glycol prepared from coal are burnt in an incinerator, and after the waste gas and waste liquid are burnt in the incinerator, flue gas is generated, and enters an SCR reactor through a flue, and nitrogen oxide is catalytically reduced into N in the SCR reactor 2 And H 2 O, simultaneously catalytically cracking dioxin into CO 2 、H 2 O and HCl; the flue gas flowing out of the SCR reactor is divided into two paths, one path enters the washing device, the other path enters the circulating blower device, and the flue gas flowing out of the circulating blower device is mixed with oxygen sent by the oxygen supply system in the combustion-supporting gas mixer to obtain combustion-supporting flue gas; the combustion-supporting flue gas enters the incinerator to be continuously combusted with the waste gas and the waste liquid.
Further, the waste gas comprises one or more of waste gas PSA tail gas, methanol rectification tail gas and DMO section MN regeneration tower tail gas; the waste liquid comprises one or more of MF waste liquid at the top of an MF separation tower in a DMO rectification section and MF light fraction waste liquid at the top of a light component removal tower in a DMC recovery section.
Further, the volume concentration of oxygen sent by the oxygen supply system is greater than or equal to 50%; the volume concentration of oxygen in the combustion-supporting flue gas is 21% -30%.
Further, the combustion temperature in the incinerator is 1100-1280 ℃; and the flue gas generated in the incinerator is cooled to 320-410 ℃ by a heat recovery device.
Further, the chemical reaction of the combustion of the waste gas and liquid in the incinerator:
methyl formate combustion: HCOOCH 3 +2O 2 =2CO 2 +2H 2 O；
Methane combustion: ch4+2o 2 =CO 2 +2H 2 O；
Dimethoxy methane combustion: c (C) 3 H 8 O 2 +4O 2 =3CO 2 +4H 2 O；
Methyl nitrite combustion: 4CH (4 CH) 3 OON+7O 2 =4CO 2 +4NO 2 +6H 2 O；
Methanol combustion: 2CH 3 OH+3O 2 =2CO 2 +4H 2 O；
Methyl nitrite decomposition: 2CH 3 ONO=HCHO+2NO+CH 3 OH；
Hydrogen combustion: 2H (H) 2 +O 2 =2H 2 O；
Nitric oxide: 2NO+O 2 =2NO 2 ；
Dimethyl carbonate: c (C) 3 H 6 O 3 +3O 2 =3CO 2 +3H 2 O；
Denitration reaction: 6NO 2 +8NH 3 =7N 2 +12H 2 O，4NH 3 +4NO+O 2 =4N 2 +6H 2 O。
The SNCR is a selective non-catalytic reduction reaction; SCR is a selective catalytic reduction reaction.
Advantageous effects
1. According to the invention, by arranging the oxygen supply system, the combustion-supporting gas mixer and the circulating blower device, flue gas generated by combustion of the incinerator enters the SCR reactor for denitration, the flue gas after denitration flows out of the SCR reactor and is divided into two parts, one part of flue gas is mixed with oxygen in the combustion-supporting gas mixer to obtain combustion-supporting flue gas, the combustion-supporting flue gas enters the incinerator for continuous incineration reaction, and the other part of flue gas enters the washing device for washing and is discharged to the atmosphere from a chimney; according to the requirements of the emission standard of atmospheric pollutants of a thermal power plant GB13223-2011 and the comprehensive emission standard of atmospheric pollutants GB 16297-1996, the concentration of NOx in the flue gas discharged to the atmosphere is not changed, but the flow of the flue gas discharged to the atmosphere is reduced, so that the total amount of the NOx discharged to the atmosphere is reduced, and the environment is effectively protected.
2. According to the invention, a part of flue gas flowing out of the SCR reactor is mixed with oxygen to be used as combustion-supporting flue gas to enter the incinerator to participate in the incineration reaction, and compared with air used as fuel gas, a preheater is not required to be arranged, so that heat consumption is reduced, heat loss carried by the part of flue gas is avoided, the part of heat is recycled, and heat loss is reduced.
3. According to the invention, a part of flue gas flowing out of the SCR reactor enters the circulating blower device, so that the flue gas quantity entering the washing device is reduced, and the flue gas entering the washing device also needs to be cooled before or during washing.
4. According to the requirement of the integrated emission standard of atmospheric pollutants GB 16297-1996 on the highest allowable emission rate of NOx, compared with air serving as fuel gas, the invention has the advantages of less NOx emission, reduced design height of an exhaust barrel or an exhaust chimney and reduced investment cost.
5. The invention utilizes the smoke circulation generated by combustion and supplements oxygen needed by the combustion in the circulated smoke to obtain combustion-supporting smoke, when the oxygen supply system of the invention provides high-purity oxygen, N in the combustion-supporting smoke 2 The ratio of the ratio is very small, and compared with the air serving as the fuel gas, when the waste gas and the waste liquid are burnt in the incinerator, the generated amount of thermal NOx and rapid NOx is reduced, so that the loads of the SNCR device and the SCR reactor are lightened, and the content of NOx in the flue gas discharged by the washing device is reduced.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
FIG. 2 is a process flow diagram of the present invention;
1-an incinerator; a 2-SCR reactor; 3-a recycle blower device; a 4-oxygen supply system; a 5-fuel supply system; 6-washing device and 7-combustion-supporting gas mixer.
Description of the embodiments
Example 1
Referring to fig. 1 and 2, in order to remove waste generated in a process for producing ethylene glycol from coalThe gas waste liquid is reasonably incinerated, so that the harm to the environment is furthest reduced during incineration, the heat loss caused by the discharge of a large amount of flue gas is furthest reduced, the consumption of heat and cold in the incineration process is reduced, and the heat recycling rate of waste gas and waste liquid incineration is improved; the invention provides a device for incinerating waste gas and waste liquid in a coal-to-ethylene glycol process, which comprises an incinerator 1, a fuel supply system 5, an SCR reactor 2, a washing device 6, a circulating blower device 3 and an oxygen supply system 1; the incinerator 1 is used for incinerating waste gas and waste liquid generated in the coal-to-ethylene glycol; the SCR reactor 2 is used for catalyzing and reducing nitrogen oxide in the flue gas into N 2 And H 2 O, simultaneously catalytically cracking dioxin in flue gas into CO 2 、H 2 O and HCl; the fuel inlet of the incinerator 1 is connected with a fuel supply system 5 through a pipeline; the combustion-supporting gas inlet of the incinerator 1 is connected to the outlet of the circulating blower device 3 through a pipeline and a combustion-supporting gas mixer 7, and the combustion-supporting gas mixer 7 is also connected to the oxygen supply system 1 through a pipeline; the oxygen supply system 1 is also provided with a standby oxygen supply system; the circulating blower device 3 is also provided with an air inlet; the combustion-supporting gas mixer 7 is used for uniformly mixing the circulating flue gas and oxygen; an online oxygen analyzer a is arranged on a pipeline connected with the outlet of the circulating blower device 3 of the combustion-supporting gas mixer 7 and used for observing the oxygen content in the flue gas flowing out of the circulating blower device 3 in real time, and an online oxygen analyzer b is arranged on a pipeline connected with the combustion-supporting gas mixer 7 of the incinerator 1 and used for observing the oxygen content in the flue gas flowing out of the combustion-supporting gas mixer 7 in real time; the flue gas outlet of the incinerator 1 is connected to the inlet of the SCR reactor 2 through a flue, and a heat recovery device is further arranged on the flue connected with the inlet of the SCR reactor 2; the heat recovery device is used for recovering heat of flue gas generated in the incinerator 1; the flue gas outlet of the SCR reactor 2 is respectively connected to the inlet of the circulating blower device 3 and the inlet of the washing device 6 in two paths through a flue; the washing device 6 is a washing tower, the washing tower is filled with filler, a washing liquid inlet and a circulating washing liquid inlet are arranged at the upper part of the washing tower, and the circulating washing liquid inlet is connected with the washing liquid through a pipelineThe circulating pump is connected to the bottom of the washing tower, and the outlet of the washing liquid circulating pump is also connected with the washing liquid discharge pipeline.
The heat recovery device comprises a high-temperature heat recovery device and a low-temperature heat recovery device; the low-temperature heat recovery device is a superheater, and the low-temperature heat recovery device is a boiler.
The fuel supply system 5 comprises a natural gas supply system, an exhaust gas supply system and a waste liquid supply system.
The flue that burns burning furnace 1 and SCR reactor 2 are connected, the flue that SCR reactor 2 and recycle blower device 3 are connected and the flue that recycle blower device 3 and burns burning furnace 1 are connected all set up the drain valve in the low-lying department for the comdenstion water of discharge flue low-lying department.
A waste gas and waste liquid incineration process method in a coal glycol process comprises the following steps:
waste gas and waste liquid generated in the coal-made glycol are burnt in the incinerator 1, the waste gas and waste liquid are burnt in the incinerator 1 to generate smoke, the smoke enters the SCR reactor 2 through a flue, and the oxynitride is catalytically reduced into N in the SCR reactor 2 2 And H 2 O, simultaneously catalytically cracking dioxin into CO 2 、H 2 O and HCl; the flue gas flowing out of the SCR reactor 2 is divided into two paths, one path enters a washing device 6, the other path enters a circulating blower device 3, and the flue gas flowing out of the circulating blower device 3 is mixed with oxygen sent by an oxygen supply system 1 in a combustion-supporting gas mixer 7 to obtain combustion-supporting flue gas; the combustion-supporting flue gas enters the incinerator 1 to be combusted with waste gas and waste liquid continuously.
The waste gas comprises PSA tail gas, methanol rectification tail gas and MN regeneration tower tail gas of a DMO section, wherein the heat value of the PSA tail gas is 13.37MJ/Nm, and the PSA tail gas can be combusted in a self-sustaining manner; the heat value of the methanol tail gas and the MN tail gas is lower, namely 1.938MJ/Nm and 2.065MJ/Nm respectively, the self-sustaining combustion cannot be realized, and the MN regeneration tower tail gas contains 0.6 percent of N by volume 2 O。
The waste liquid comprises MF waste liquid at the top of a MF separation tower in a DMO rectification section and MF light fraction waste liquid at the top of a light removal tower in a DMC recovery section, and has high heat values of 18.25 and 17.37 MJ/kg respectively, no other inert substances and easy combustion; the MF waste liquid contains methyl nitrite, and the substance is explosive, has primary sensitivity and detonates at 140 ℃ and prevents the explosion in the combustion of the MF waste liquid.
The incinerator 1 adopts PSA tail gas as main fuel, and simultaneously incinerates 4420 Nm/h MN regeneration tower tail gas and 240 Nm/h methanol rectification tail gas in a DMO working section; the incinerator 1 is provided with a waste liquid spray gun, and can treat 1601kg/h MF light fraction waste liquid and 919kg/h MF waste liquid; during normal operation, PSA tail gas is used as main fuel, and natural gas is used as stable combustion fuel; when the PSA tail gas supply fails, the fuel gap is replenished by natural gas;
the high-temperature heat recovery device can heat 9.8MPa saturated steam to about 540 ℃ to generate superheated steam; 9.8MPa saturated steam supply fails, and waste gas, waste liquid or natural gas supply is correspondingly regulated; when the 9.8MPa saturated steam supply is less than 30% of the design load, the system is shut down.
The operation temperature of the incinerator 1 is controlled to be 1100-1280 ℃, the residence time is not less than 2 seconds, and the residence time is counted from the last injection port of the waste gas so as to ensure that all harmful substances and organic components are completely incinerated; the industrial multi-medium low-nitrogen burner is combined, and the amount of thermal NOx and fuel type NOx generated by burning the waste gas and the waste liquid is reduced by grading combustion-supporting smoke, grading waste gas and waste liquid and circulating various low-nitrogen combustion of the smoke.
The flue gas from the incinerator 1 enters a high-temperature heat recovery device, and saturated steam of 9.8MPa is heated to superheated steam of about 540 ℃ in the high-temperature heat recovery device; an SNCR device is arranged in the high-temperature heat recovery device, ammonia water with the mass concentration of 19% -21% is sprayed into the SNCR device at the temperature of 850-1050 ℃ to perform selective reaction with NOx, so that the NOx is reduced into N 2 And H 2 O, removing 30% -40% of NOx; the volume concentration of ammonia in the air reaches 16% -25%, so that explosion can occur when the ammonia meets open fire; the most ignition concentration of 17% is more dangerous if oils or other combustible materials are present, and the concentration of ammonia is controlled to be well below the lower explosion limit, typically 5% during operation.
After passing through the high-temperature heat recovery device, the high-temperature flue gas still contains high heat to be recovered at 497 ℃, so that the low-temperature heat recovery device is arranged behind the high-temperature heat recovery device, the heat recovery rate is improved, and the energy-saving requirement is met. The temperature of the flue gas is reduced to 320-410 ℃ through a low-temperature heat recovery device; the flue gas enters the SCR reactor 2 after being subjected to denitration in the SCR reactor 2 is divided into two parts, one part enters the circulating blower device 3, the other part enters the washing tower after being cooled, and the flue gas is discharged into the atmosphere from a chimney after being washed by the washing tower.
The natural gas supply system is divided into three paths, wherein the first path of natural gas is used for igniting and burning a pilot burner, the second path of natural gas is used for starting a burner and adjusting load, and the third path of natural gas is used for a natural gas spray gun group of the auxiliary burner; the natural gas supply pipeline is provided with measuring and controlling elements such as a self-operated pressure regulating valve, a pneumatic diaphragm regulating valve, a quick cut-off valve, a flame arrester, a flowmeter, a pressure gauge and the like.
The waste gas supply system comprises a PSA tail gas system, a methanol rectification tail gas system and an MN regeneration tower tail gas system;
the PSA tail gas system comprises a blind plate, a cut-off valve, a pneumatic diaphragm regulating valve, a double quick cut-off valve, a flame arrester, a flowmeter, a pressure gauge and other measuring and controlling elements which are arranged on a PSA tail gas supply pipeline; the PSA tail gas is used as main fuel to provide energy for the incineration of other low-heat-value waste gases.
The PSA tail gas system is provided with a fire removing torch bypass pipeline, and a pneumatic regulating valve with regulating and cutting-off functions is arranged on the bypass pipeline; when the PSA tail gas supply amount is larger than the required amount of the incinerator 1, the PSA tail gas is discharged from the fire-removing torch; the bypass of the flame removing torch of the PSA tail gas system is also provided with double quick cut-off valves, a nitrogen seal is arranged between the double quick cut-off valves, when the system fails, the PSA tail gas can be prevented from leaking into the incinerator 1, a pressure switch is arranged between the double valves, and the effectiveness of the nitrogen seal is monitored.
The methanol rectifying tail gas system and the MN regeneration tower tail gas system respectively enter the incinerator 1 for incineration through two pipelines, and measuring and controlling elements such as a double-quick cut-off valve, a flowmeter, a pressure gauge, a pressure transmitter and the like are arranged on the two pipelines; the two pipelines are provided with a fire removing torch bypass, and the two bypass pipelines are provided with pneumatic valves with cutting-off functions; when the waste gas and waste liquid incineration system fails, the waste gas is diffused by the fire-removing torch; a nitrogen seal is arranged between the two quick shut-off valves, so that waste gas is prevented from leaking into the incinerator 1 when a system fails; a pressure switch is arranged between the two valves to monitor the effectiveness of the nitrogen seal.
The waste liquid supply system comprises a waste liquid pipeline and measuring and control elements such as a double quick cut-off valve, a flowmeter, a pressure gauge, a pressure transmitter and the like which are arranged on the waste liquid pipeline, wherein the waste liquid enters the incinerator 1 for incineration after passing through the control valve group, and the waste liquid adopts saturated steam and compressed N 2 Atomization is carried out, wherein the MF waste liquid is compressed by N 2 Saturated steam is used for MF light fraction waste liquid; the saturated steam is decompressed from the saturated steam of the medium-pressure waste heat boiler of the device.
PSA tail gas is the main heat source of the device, but the fluctuation of the load of the PSA device can cause the pressure and flow of the PSA tail gas to change; in order to reduce the influence of fluctuation of the PSA device on a combustion system, the incinerator 1 is provided with a main burner and an auxiliary burner; the heat load of the main burner is equivalent to 20% -30% of the total load, a small amount of natural gas and 2000Nm PSA tail gas are combusted, and the main burner is responsible for providing a stable high-temperature ignition source for the auxiliary burner; the auxiliary burner is provided with an independent PSA tail gas spray gun and a natural gas spray gun, the natural gas spray gun is used for standby, and when the PSA tail gas spray gun cannot provide enough fuel, the natural gas spray gun provides notch fuel; when the operation heat load of the incinerator fluctuates, the fuel supply of the auxiliary burner is preferentially regulated, and the load of the main burner is kept stable. The heat value of the waste gas is lower, and the waste gas intensively enters the incinerator 1 to reduce the flame temperature and influence the combustion stability, so that the waste gas enters the incinerator 1 in the middle position of combustion and the temperature rise and ignition are completed by high-temperature flue gas.
The waste liquid spray gun enters the incinerator 1 in the middle of the combustion chamber, ignition is realized by means of hot flue gas and heat radiation of a high-temperature hearth, the waste liquid spray gun is uniformly arranged along the circumference of the combustion chamber, the waste liquid contains explosives with primary sensitivity, when the waste liquid is not combusted in normal conditions, no fuel is arranged in the waste liquid spray gun for cooling, in order to ensure the safety of waste liquid combustion, the waste liquid spray gun adopts an air-cooled waste liquid spray gun, the outermost layer of the air-cooled waste liquid spray gun is an air-cooled jacket, cold compressed air flows in the jacket, heat transferred to the spray gun by the hearth is taken away, and the temperature of the spray gun is ensured not to exceed 100 ℃.
The incinerator 1 is also provided with an ignition device, and the ignition device comprises an electric ignition rod, an ignition transformer and an automatic flame monitor; the ignition rod is an ignition device used by a compressed gas type flame thrower, is generally arranged at a spray gun port and can ignite for a plurality of times; the ignition transformer has two sets of coils, a primary coil and a secondary coil. The primary coil is wound by a thicker enameled wire, usually by about 200-500 turns by using an enameled wire of about 0.5-1.0 mm; the secondary coil is wound by a thinner enameled wire, usually by an enameled wire of about 0.1mm for about 15000-25000 turns; one end of the primary coil is connected with the positive electrode of the low-voltage power supply, and the other end of the primary coil is connected with a switching device which is a breaker; one end of the secondary coil is connected with the primary coil, and the other end of the secondary coil is connected with the output end of the high-voltage wire to output high-voltage power; the flame monitor, also called an electric eye, is a device that sends a flame presence, flame extinction or interruption signal to a control device, and generally consists of a sensor and a controller.
The superheater is provided with three-stage superheating, and a desuperheater with good regulation performance is arranged in the superheater; in order to avoid excessive thermal stress caused by direct contact of sprayed water drops and a steam pipeline, the desuperheater is provided with a protective sleeve at the water spraying position; the design temperature regulating amplitude of the desuperheater is more than 50 ℃, and a back flushing pipeline is arranged; the superheater is provided with a tube seat for emptying and draining, a pipeline and a valve; the drainage of the superheater header is to adopt bilateral drainage;
the superheater outlet header can bear certain thrust and moment from the main steam pipeline and is arranged in coordination with the main pipeline system; the low-temperature superheater for convective heat transfer is made of 12Cr1MoVG material, and the medium-temperature and high-temperature superheater is made of SA213-T91 material; the material of the high-temperature superheater steam pipeline is SA355M-P91.
The circulating blower device 3 comprises a primary blower, a secondary blower and a tertiary blower, wherein the primary blower, the secondary blower and the tertiary blower are variable-frequency blowers and are all formed by connecting two blowers in parallel, one blower is used for one purpose, the failed blower can be rapidly isolated when one blower fails, the standby blower is started, the primary blower, the secondary blower and the tertiary blower are all provided with air inlets, the air inlets are provided with silencers and dust covers, the dust covers prevent a large amount of dust from entering the incineration system, the device is blocked, and the outlet is provided with a flowmeter and a regulating air door.
The oxygen supply system 1 further comprises a blind plate, a cut-off valve, a regulating valve, a double quick cut-off valve, a flowmeter, a pressure gauge and other measuring and controlling elements which are arranged on a connecting pipeline of the fuel gas mixer 7 and the oxygen supply system; a nitrogen seal is arranged between the double quick cut-off valves, so that oxygen can be prevented from leaking into the incinerator 1 when the system fails, a pressure switch is arranged between the double valves, and the effectiveness of the nitrogen seal is monitored; the oxygen supply system 1 is also provided with a standby oxygen supply system to prevent the standby oxygen supply system from providing oxygen to the incinerator when the oxygen supply system 1 fails.
When the incinerator is started, natural gas is firstly used as fuel, air is used as combustion-supporting substance, smoke is generated by combustion, the frequency conversion of the blower and the air damper at the outlet of the blower are slowly and gradually adjusted, one part of smoke is circularly fed into the incinerator 1, the other part of smoke is washed by the washing tower and then is discharged, the smoke enters the incinerator 1, and the adjusting valve of the oxygen supply system 1 is adjusted to mix oxygen with the smoke, the volume concentration of oxygen sent by the oxygen supply system 1 is 50%, and the reduction of the oxygen content in the combustion-supporting substance is avoided; the method comprises the steps of gradually increasing the circulation amount of flue gas, and simultaneously, feeding waste gas and waste liquid into the incinerator 1 for combustion, wherein the waste gas and the waste liquid are firstly fed into the incinerator 1 from flammable waste gas and waste liquid according to the difficulty of combustion, and then fed into the incinerator 1 from waste gas and waste liquid difficult to combust; when the amount of waste gas and waste liquid entering the incinerator 1 is gradually increased, the smoke generated by combustion is more and more, the entering amount of air slowly exits until the air completely exits, at the moment, the combustion-supporting substance of the incinerator 1 is combustion-supporting smoke, oxygen in the combustion-supporting smoke is supplied by the oxygen supply system 1, and the volume concentration of the oxygen in the combustion-supporting smoke is 21%; the circulation amount of the combustion-supporting flue gas is controlled according to the amount of waste gas and waste liquid.
Another embodiment differs from embodiment 1 in that: the volume concentration of oxygen sent by the oxygen supply system 1 is 60%; the volume concentration of oxygen in the combustion-supporting flue gas is 23%; the waste gas comprises waste gas PSA tail gas and DMO section MN regeneration tower tail gas; the waste liquid comprises MF waste liquid at the top of an MF separation tower in a DMO rectification section and MF light fraction waste liquid at the top of a light component removal tower in a DMC recovery section.
Another embodiment differs from embodiment 1 in that: the oxygen volume concentration sent by the oxygen supply system 1 is 70%; the volume concentration of oxygen in the combustion-supporting flue gas is 27%; the waste gas comprises waste gas PSA tail gas and methanol rectification tail gas; the waste liquid comprises MF waste liquid at the top of an MF separation tower in a DMO rectification section and MF light fraction waste liquid at the top of a light component removal tower in a DMC recovery section.
Another embodiment differs from embodiment 1 in that: the oxygen volume concentration sent by the oxygen supply system 1 is 80%; the volume concentration of oxygen in the combustion-supporting flue gas is 30%; the waste gas comprises waste gas PSA tail gas, methanol rectification tail gas and MN regeneration tower tail gas in a DMO working section; the waste liquid comprises MF light fraction waste liquid at the top of the light component removing tower in the DMC recovery section.
Another embodiment differs from embodiment 1 in that: the volume concentration of oxygen sent by the oxygen supply system 1 is 90%; the volume concentration of oxygen in the combustion-supporting flue gas is 21%; the waste gas comprises waste gas PSA tail gas, methanol rectification tail gas and MN regeneration tower tail gas in a DMO working section; the waste liquid comprises MF waste liquid at the top of an MF separation tower in a DMO rectification section.
Another embodiment differs from embodiment 1 in that: the oxygen volume concentration sent by the oxygen supply system 1 is 99%; the volume concentration of oxygen in the combustion-supporting flue gas is 21%; the exhaust gas comprises exhaust PSA tail gas; the waste liquid comprises MF waste liquid at the top of an MF separation tower in a DMO rectification section and MF light fraction waste liquid at the top of a light component removal tower in a DMC recovery section.
The working principle of the invention is as follows: according to the invention, through arranging the oxygen supply system 1, the combustion-supporting gas mixer 7 and the circulating blower device 3, flue gas generated by combustion of the incinerator 1 sequentially flows through the heat recovery device and the SCR reactor 2, the flue gas flowing out of the SCR reactor 2 is divided into two parts, one part of flue gas is mixed with oxygen in the combustion-supporting gas mixer 7 to obtain combustion-supporting flue gas, the combustion-supporting flue gas enters the incinerator 1 to continue to perform incineration reaction, and the other part of flue gas enters the washing device 6 to be washed and then is discharged to the atmosphere from a chimney; according to the emission standard of atmospheric pollutants of thermal power plantsAccording to the requirements of GB13223-2011 and GB 16297-1996 on comprehensive emission standards of atmospheric pollutants, the concentration limit value of NOx in the flue gas discharged to the atmosphere is 50mg/m, compared with the air serving as a fuel gas, the invention still limits the emission according to the NOx, but the flow of the flue gas discharged to the atmosphere is greatly reduced, so that the total amount of NOx discharged to the atmosphere is reduced, and the environment is effectively protected; according to the invention, a part of flue gas flowing out of the SCR reactor 2 is mixed with oxygen to serve as combustion-supporting flue gas to enter the incinerator 1 to participate in the incineration reaction, and compared with air serving as fuel gas, a preheater is not needed, so that heat consumption is reduced, heat loss carried by the part of flue gas is avoided, the part of heat is recycled, and heat loss is reduced; meanwhile, part of the flue gas flowing out of the SCR reactor 2 enters the circulating blower device 3, so that the flue gas quantity entering the washing device 6 is reduced, and the flue gas entering the washing device 6 needs to be cooled before or during washing; according to the requirement of the integrated emission standard of atmospheric pollutants GB 16297-1996 on the highest allowable emission rate of NOx, compared with air serving as fuel gas, the invention has the advantages that the emission amount of NOx is less, thereby reducing the design height of an exhaust barrel or an exhaust chimney and reducing the investment cost; the invention utilizes the smoke circulation generated by combustion and supplements oxygen needed by the combustion in the circulated smoke to obtain combustion-supporting smoke, when the oxygen supply system 1 of the invention provides high-purity oxygen, N in the combustion-supporting smoke 2 The ratio is extremely small, and when the waste gas and the waste liquid are burnt in the incinerator 1, compared with the air serving as the fuel gas, the generated amount of thermal NOx and rapid NOx is reduced, so that the loads of the SNCR device and the SCR reactor 2 are lightened, and the content of NOx in the flue gas discharged by the washing device 6 is reduced.
Modifications and variations of this invention will be apparent to those skilled in the art and are intended to be within the scope of the invention and are not limited to the embodiments described.
Claims (10)
1. Waste gas and waste liquid incineration device in coal-to-ethylene glycol processThe device comprises an incinerator, a fuel supply system, an SCR reactor and a washing device, wherein the incinerator is used for incinerating waste gas and waste liquid generated in the coal-to-ethylene glycol; the fuel inlet of the incinerator is connected with the fuel supply system through a pipeline; the SCR reactor is used for catalyzing and reducing nitrogen oxide compounds in the flue gas into N 2 And H 2 O, simultaneously catalytically cracking dioxin in flue gas into CO 2 、H 2 O and HCl; the method is characterized in that: the device also comprises a circulating blower device and an oxygen supply system; the combustion-supporting gas inlet of the incinerator is connected to the outlet of the circulating blower device through a pipeline and a combustion-supporting gas mixer, and the combustion-supporting gas mixer is also connected to an oxygen supply system through a pipeline; the combustion-supporting gas mixer is used for uniformly mixing the circulating smoke and oxygen; the flue gas outlet of the incinerator is connected to the inlet of the SCR reactor through a flue; the flue gas outlet of the SCR reactor is respectively connected to the inlet of the circulating blower device and the inlet of the washing device in two paths through a flue.
2. The device for incinerating waste gas and waste liquid in a process for preparing ethylene glycol from coal according to claim 1, wherein: a flue with a flue gas outlet of the incinerator connected with an inlet of the SCR reactor is also provided with a heat recovery device; the heat recovery device is used for recovering heat of flue gas generated in the incinerator; and the pipeline connected with the combustion-supporting gas mixer of the incinerator and the pipeline connected with the outlet of the circulating blower device of the combustion-supporting gas mixer are both provided with an online oxygen analyzer.
3. The device for incinerating waste gas and waste liquid in a process for preparing ethylene glycol from coal according to claim 1, wherein: the circulating blower device is formed by connecting a plurality of blowers in parallel, and each blower is provided with an air inlet.
4. The device for incinerating waste gas and waste liquid in the process of preparing ethylene glycol from coal according to claim 2, wherein: the heat recovery device comprises a high-temperature heat recovery device and a low-temperature heat recovery device; the low-temperature heat recovery device is a superheater, and the low-temperature heat recovery device is a boiler; and an SNCR device is arranged in the high-temperature heat recovery device.
5. The device for incinerating waste gas and waste liquid in a process for preparing ethylene glycol from coal according to claim 1, wherein: the fuel supply system comprises a natural gas supply system, an exhaust gas supply system and a waste liquid supply system, and bypass pipelines for removing the torch are arranged.
6. The device for incinerating waste gas and waste liquid in a process for preparing ethylene glycol from coal according to claim 5, wherein: the natural gas supply system, the waste gas supply system and the waste liquid supply system are respectively provided with a pipeline which is communicated with a spray gun in the incinerator; the oxygen supply system is provided with a standby oxygen supply system.
7. A waste gas and waste liquid incineration process method in a coal glycol process is characterized in that: the waste gas and waste liquid incineration process method in the coal-to-ethylene glycol process is performed by adopting the waste gas and waste liquid incineration device in the coal-to-ethylene glycol process according to any one of claims 1-5, and comprises the following steps:
waste gas and waste liquid generated in the ethylene glycol prepared from coal are burnt in an incinerator, and after the waste gas and waste liquid are burnt in the incinerator, flue gas is generated, and enters an SCR reactor through a flue, and nitrogen oxide is catalytically reduced into N in the SCR reactor 2 And H 2 O, simultaneously catalytically cracking dioxin into CO 2 、H 2 O and HCl; the flue gas flowing out of the SCR reactor is divided into two paths, one path enters the washing device, the other path enters the circulating blower device, and the flue gas flowing out of the circulating blower device is mixed with oxygen sent by the oxygen supply system in the combustion-supporting gas mixer to obtain combustion-supporting flue gas; the combustion-supporting flue gas enters the incinerator to be continuously combusted with the waste gas and the waste liquid.
8. The method for incinerating waste gas and waste liquid in the process of preparing ethylene glycol from coal, which is characterized in that: the waste gas comprises one or more of waste gas PSA tail gas, methanol rectification tail gas and DMO section MN regeneration tower tail gas; the waste liquid comprises one or more of MF waste liquid at the top of an MF separation tower in a DMO rectification section and MF light fraction waste liquid at the top of a light component removal tower in a DMC recovery section.
9. The method for incinerating waste gas and waste liquid in the process of preparing ethylene glycol from coal, which is characterized in that: the volume concentration of oxygen sent by the oxygen supply system is more than or equal to 50%; the volume concentration of oxygen in the combustion-supporting flue gas is 21% -30%.
10. The method for incinerating waste gas and waste liquid in the process of preparing ethylene glycol from coal, which is characterized in that: the combustion temperature in the incinerator is 1100-1280 ℃; and the flue gas generated in the incinerator is cooled to 320-410 ℃ by a heat recovery device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310230945.1A CN116293742A (en) | 2023-03-12 | 2023-03-12 | Device and process method for incinerating waste gas and waste liquid in process of preparing ethylene glycol from coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310230945.1A CN116293742A (en) | 2023-03-12 | 2023-03-12 | Device and process method for incinerating waste gas and waste liquid in process of preparing ethylene glycol from coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116293742A true CN116293742A (en) | 2023-06-23 |
Family
ID=86812684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310230945.1A Pending CN116293742A (en) | 2023-03-12 | 2023-03-12 | Device and process method for incinerating waste gas and waste liquid in process of preparing ethylene glycol from coal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116293742A (en) |
-
2023
- 2023-03-12 CN CN202310230945.1A patent/CN116293742A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101761978B1 (en) | Method and apparatus for reducing nox emissions in the incineration of tail gas | |
| US20030097840A1 (en) | Koh flue gas recirculation power plant with waste heat and byproduct recovery | |
| EP0521949B1 (en) | IMPROVED LOW NOx COGENERATION PROCESS AND SYSTEM | |
| US4811555A (en) | Low NOX cogeneration process | |
| CN105937766A (en) | Low nitrogen oxide incinerating device used for treatment of nitrogen containing waste gas and nitrogen containing waste liquid and low nitrogen oxide incinerating method used for treatment of nitrogen containing waste gas and nitrogen containing waste liquid | |
| US5178101A (en) | Low NOx combustion process and system | |
| CN113623665B (en) | System and method for incinerating waste gas and waste liquid of ethylene glycol device | |
| CN112283725A (en) | Direct combustion type waste gas incineration system process | |
| CN211098341U (en) | SCR flue gas denitration device of garbage incinerator | |
| CA2830559C (en) | Cogeneration power plant | |
| CN219913084U (en) | Waste gas and waste liquid incineration device in coal-to-ethylene glycol process | |
| CN103398397A (en) | Combustion system of boiler and combustion method implemented by aid of system | |
| EP2065570B1 (en) | Burner for generating reductive atmosphere of exhaust gas in engine cogeneration plant having denitrification process | |
| CN116293742A (en) | Device and process method for incinerating waste gas and waste liquid in process of preparing ethylene glycol from coal | |
| CN112275108B (en) | Sintering flue gas cooperative treatment system, flue gas treatment method and application | |
| CN205842694U (en) | A kind of low NOx incinerator processing nitrogenous waste gas, waste liquid | |
| CN113154365A (en) | Supercritical CO2Experimental system for coal-fired boiler ultralow emission research | |
| JPH01193513A (en) | Method of simultaneously generating low nox | |
| CN114811616A (en) | Burner, device and process for thermal oxidation incineration treatment of HCN-containing waste gas | |
| KR101102062B1 (en) | a NOx reducing system of using burner with a high pressure and an air current | |
| CN220981352U (en) | Waste gas and waste liquid treatment system | |
| CN221505022U (en) | Temperature-controllable heat accumulating type thermal oxidation device | |
| CN214470006U (en) | Low-nitrogen combustion system of gas type tunnel kiln | |
| KR200199659Y1 (en) | Improvement of boiler exhaust gas purifier | |
| CN221958877U (en) | Combined device for high-concentration organic waste gas and waste liquid incineration and purification |
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 |