CN101138699A - Method and equipment for treating tail gas pollution of absorption tower of acrylonitrile device - Google Patents
Method and equipment for treating tail gas pollution of absorption tower of acrylonitrile device Download PDFInfo
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- CN101138699A CN101138699A CNA2006101128347A CN200610112834A CN101138699A CN 101138699 A CN101138699 A CN 101138699A CN A2006101128347 A CNA2006101128347 A CN A2006101128347A CN 200610112834 A CN200610112834 A CN 200610112834A CN 101138699 A CN101138699 A CN 101138699A
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- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 13
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000000945 filler Substances 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 36
- 238000007084 catalytic combustion reaction Methods 0.000 claims abstract description 18
- 239000002912 waste gas Substances 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 239000002918 waste heat Substances 0.000 claims abstract description 11
- 239000000919 ceramic Substances 0.000 claims abstract description 6
- 238000009434 installation Methods 0.000 claims description 13
- 230000000694 effects Effects 0.000 claims description 7
- 229910052573 porcelain Inorganic materials 0.000 claims description 6
- -1 and savings therein Substances 0.000 claims description 5
- 239000000376 reactant Substances 0.000 claims description 5
- 239000005416 organic matter Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 238000009825 accumulation Methods 0.000 claims description 3
- 239000004480 active ingredient Substances 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 239000010970 precious metal Substances 0.000 claims description 3
- 238000004901 spalling Methods 0.000 claims description 3
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 16
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 15
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 abstract description 6
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 150000001875 compounds Chemical class 0.000 abstract 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract 2
- 239000004215 Carbon black (E152) Substances 0.000 abstract 1
- 239000006185 dispersion Substances 0.000 abstract 1
- 239000000463 material Substances 0.000 abstract 1
- 239000002245 particle Substances 0.000 abstract 1
- 239000008188 pellet Substances 0.000 abstract 1
- 230000000737 periodic effect Effects 0.000 abstract 1
- 239000000843 powder Substances 0.000 abstract 1
- 238000009827 uniform distribution Methods 0.000 abstract 1
- 239000011800 void material Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 18
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 16
- 239000001294 propane Substances 0.000 description 8
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 8
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 8
- 238000004088 simulation Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 230000000454 anti-cipatory effect Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- XLJMAIOERFSOGZ-UHFFFAOYSA-N cyanic acid Chemical compound OC#N XLJMAIOERFSOGZ-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N Acrylic acid Chemical compound OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- 235000007871 Chrysanthemum coronarium Nutrition 0.000 description 1
- 244000067456 Chrysanthemum coronarium Species 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- HGINCPLSRVDWNT-UHFFFAOYSA-N acrylaldehyde Natural products C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000003863 metallic catalyst Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Catalysts (AREA)
Abstract
The invention relates to a method and equipment for treating organic, inorganic and cyanogen-containing compound waste gas discharged from an absorption tower of an acrylonitrile device, which is characterized in that a tail gas treatment device of flow direction conversion catalytic combustion equipment consisting of two groups of periodic automatic control pneumatic or electric valves, two fixed bed reactors, a waste heat boiler or a heat exchanger is added at the tail gas part of the absorption tower of the acrylonitrile device, a catalyst is prepared by a method with high dispersion rate and uniform distribution, and the particle size is as follows: phi 3-10 mm, compressive strength: not less than 50N/pellet, bulk density: 0.55-0.95 kg/l, specific surface: 250m2A catalyst per gram; the filler is regular ceramic filler, the bed layer void ratio is 60-70%, and the specific surface area is 300-400 m2/m3The weight of the powder is 500 to 950kgf/m3Or a ceramic ring and a ceramic ball, the temperature rapid change (DEG C) resistance is more than 500, and the volume ratio of the filling material and the catalyst in the reactor is as follows: the ratio of the upper layer filler to the catalyst to the lower layer filler is 0.1-0.2: 1: 2-6, the removal rate of the non-methane total hydrocarbon reaches 97%, and the acrylonitrileThe removal rate of cyanogen-containing compounds reaches 98 percent, and the removal rate of carbon monoxide reaches 98 percent.
Description
Technical field:
The present invention relates to a kind of method and apparatus organic, that inorganic pollution especially contains the waste gas of cyanogen compound that contains of handling the absorption tower of acrylonitrile installation discharging.
Background technology:
For the very big acrylonitrile commercial plant tail gas that contains low-concentration organic of tolerance, it is very effective adopting high temperature incineration (AOGI) method to handle.External same device adopts this method to handle mostly.The capital equipment of high temperature incineration method is 1 incinerator.Principle is that acrylonitrile absorbing tower tail gas, postcombustion and air make harmful substances such as hydro carbons in the tail gas, carbon monoxide, acrylonitrile change into carbon dioxide by flame combustion in incinerator and water is discharged into atmosphere with flue gas, the superheated steam of by-product 4.1MPa.The high-temp combustion treatment technology of U.S. PCC company is used wider, has 15 to use achievement.Two acrylonitrile factories of U.S. BP company all adopt PCC company technology.Domesticly just also will adopt the PCC technology to handle acrylonitrile absorbing tower tail gas at the Shanghai of joint construction Sai Ke petro-chemical corporation acrylonitrile installation.Anqing Petrochemical Company company acrylonitrile installation was accepted Japanese green energy program assistance in 1999 and is adopted Japanese BHK technology to build up acrylonitrile absorbing tower tail gas and waste water incineration device and heat recovery system at the bottom of calendar year 2001, and by national acceptance.But high-temperature flame technology one-time investment and operating cost height, and produce a large amount of nitrogen oxide and cause secondary pollution.
Common catalytic combustion technology (AOGC) is meant at a lower temperature (260～600) ℃, effect by catalyst, with a kind of waste gas processing method of the combustible components oxidation Decomposition in the waste gas, capital equipment is not catalytic reactor and necessary heat exchanger under having the condition of thermal-flame.External existing acrylonitrile industrial installation adopts Production by Catalytic Combustion Process to handle acrylonitrile tail gas, and domestic Dongfang Chemical Plant, Beijing, The East Chemical Plant,Beijing acroleic acid device adopts Mitsubishi heavy industry catalytic combustion technology to handle tail gas.But this technology needs postcombustion gas when tail gas concentration is low, operating cost is higher.
As a kind of novel fixed bed reactors non-steady-state operation technology, though the notion of flow-reversal catalytic combustion was just proposed by Cottrell as far back as 1938, but only equal to attempt between the seventies to the eighties it is carried out mathematical description at Boreskov and Matros, and experimental study and commercial use combine after, just make it demonstrate great vitality.After this, the research unit of many countries and university have all carried out the research of this respect, during have a large amount of articles to deliver.In recent years, more existing abroad industrialized units adopt the flow-reversal catalytic combustion technology to handle the waste gas that contains volatile organic matter (VOCs).Administer as contain methyl alcohol, phenol, formaldehyde exhaust-gas that Kemerovo in 1989 is discharged when the production of resins; The improvement that contains industrial waste gases such as acrylonitrile, cyanic acid, acetaldehyde, acetate that Navoi in 1991 is discharged in water and behind the container etc. all adopt the flow-reversal catalytic combustion technology to administer.
Summary of the invention:
The objective of the invention is to develop a kind of employing flow-reversal catalytic combustion technology and administer tail gas from absorption tower of acrylonitrile installation.
In order to achieve the above object, the present invention includes two groups of pneumatic or electrically operated valves of control periodically automatically in the increase of tail gas from absorption tower of acrylonitrile installation position, two fixed bed reactors, the exhaust gas processing device of the flow-reversal catalytic combustion equipment that waste heat boiler or heat exchanger constitute, in the middle of two fixed bed reactors is catalyst layer, two ends are the high heat capacity inert filler, by an air intake valve and the valve of giving vent to anger be one group two groups periodically automatically pneumatic the or electrically operated valve of control be connected with the fixed bed reactors bottom respectively, two reactor upper ends are connected with high temperature heat collector waste heat boiler or heat exchanger respectively, tail gas enters pipe and is connected with two groups of automatic control air intake valves pneumatic or electrically operated valve respectively, and the purified gas outlet is connected with two groups of automatic control valves of giving vent to anger pneumatic or electrically operated valve respectively; Catalyst is for adopting γ-Al
2O
3Being carrier, is main active ingredient with precious metals pt, Pd, is prepared from granularity with the equally distributed method of high dispersive rate: Φ 3-10mm, compression strength: 〉=50N/ grain, bulk density: 0.55-0.95Kg/L, specific surface :～250m
2The catalyst of/g; Filler can be selected regular ceramic packing for use, and bed voidage is 60～70%, the big 300～400m2/m of specific area
3, weight accumulation is 500～950kgf/m
3, or porcelain ring, porcelain ball, spalling resistance (℃)＞500, filler and catalyst amount in the reactor are by volume: upper strata filler: catalyst: lower floor's filler=0.1～0.2: 1: 2～6.
Technological process is:
The commutation cycle that reactant is set by the time relay alternately enters the reactor two ends from two intake valves, when the air intake valve of a reactor is opened, its valve closing of giving vent to anger, and the air intake valve of another reactor is closed, its air outlet valve is opened, gas enters the reactor of its connection from the valve of opening, at first through the inert filler of reactor upper end by heat temperature raising gradually, near the top catalyst time, reach the activity of such catalysts temperature, volatile organic matter is by catalytic combustion, through adjusting superfluous heat is taken away by waste heat boiler or heat exchanger, the high-temp waste gas that purifies enters another reactor, through the lower end inert filler with the heat transferred filler, and savings therein, gas is lowered the temperature gradually, enter blast pipe through the connected valve of giving vent to anger, after the half period that reaches time relay setting, the valve closing of opening, the valve opening of closing, reactant flows to and changes, enter another reactor, waste gas enters the catalyst section reaction through this reactor lower end inert filler, and the gas of purification is lowered the temperature after valve enters blast pipe through previous reactor lower end inert filler.The heat major part of exothermic reaction generation all is accumulated in the reactor bed like this, superfluous heat is removed by heat exchanger, reach effective utilization of heat, even still can reach self-heating operation, the Steam Recovery utilization that can produce 1～4Mpa when comhustible component is high when therefore combustible concentration is very low in the waste gas.
The flow-reversal catalytic combustion technology that the present invention adopts is administered acrylonitrile tail gas, NMHC clearance after the improvement has reached more than 97%, acrylonitrile etc. contain the cyanogen compound clearance and reach more than 98%, the carbon monoxide removal rate reaches more than 98%, and the tail gas after the improvement has reached discharging standards, and it is wide to adopt present technique to have processed tail gas combustible safe level excursion, minimum safe level is very low, once invest less, take up an area of few, characteristics such as simple to operate and operating cost is low.
Description of drawings:
Fig. 1 flow-reversal catalytic combustion is administered acrylonitrile tail gas process sketch.
Wherein: 1, air intake valve 2, air intake valve 3, the valve 4 of giving vent to anger, the valve 5 of giving vent to anger, inert filler 6, inert filler 7, catalyst 8, catalyst 9, waste heat boiler or heat exchanger 10, anticipatory electric heater 11, reactor 12, reactor 13, tail gas air inlet pipe 14, purification tracheae
Concrete real-time mode
Embodiment 1
The present invention includes two groups of pneumatic or electrically operated valves of control periodically automatically in the increase of tail gas from absorption tower of acrylonitrile installation position, two fixed bed reactors, the exhaust gas processing device of the flow-reversal catalytic combustion equipment that waste heat boiler or heat exchanger constitute, it in the middle of two fixed bed reactors catalyst (7) (8) layer, two ends are high heat capacity inert filler (5) (6), by air intake valve (1) and the valve of giving vent to anger (4), air intake valve (2) controls pneumatic automatically with two groups of periodicity that the valve of giving vent to anger (3) constitutes or electrically operated valve is connected with fixed bed reactors (11) (12) bottom respectively, two reactor upper ends are connected with waste heat boiler or heat exchanger (9) respectively, tail gas enters pipe (13) and is connected with two groups of automatic control air intake valves (1) (2) pneumatic or electrically operated valve respectively, purified gas outlet (14) is connected with two groups of automatic control valves of giving vent to anger (3) (4) pneumatic or electrically operated valve respectively, and anticipatory electric heater (10) is connected with reactor; Catalyst adopts γ-Al
2O
3Being carrier, is main active ingredient with precious metals pt, is prepared from granularity with the equally distributed method of high dispersive rate: Φ 3-10mm, compression strength: 〉=50N/ grain, bulk density: 0.55-0.95Kg/L, specific surface: 250m
2The catalyst of/g; Filler can be selected regular ceramic packing for use, and bed voidage is 60～70%, the big 300～400m2/m of specific area
3, weight accumulation is 500～950kgf/m
3, or porcelain ring, porcelain ball, spalling resistance (℃)＞500, filler and catalyst amount in the reactor are by volume: upper strata filler: catalyst: lower floor's filler=0.1～0.2: 1: 2～6.
Technological process is:
Accompanying drawing is seen in the technological process of acrylonitrile absorbing tower exhaust gas flow direction conversion catalytic combustion, and catalyst and two ends inert filler are preheated to more than the catalyst activity temperature (330 ℃), and tail gas combustible concentration is 540mg/m
3, the flow-reversal cycle is 200s, reaction velocity is 20000h
-1
The commutation cycle that reactant is set by the time relay alternately enters the reactor two ends from two intake valves (1) (2), when the air intake valve (1) of reactor (11) is opened, its valve of giving vent to anger (3) is closed, and the air intake valve (2) of reactor (12) is closed, its air outlet valve (4) is opened, gas enters the reactor (11) of its connection from the valve of opening (1), at first through the inert filler (5) of reactor upper end by heat temperature raising gradually, near top catalyst (7) time, reach the activity of such catalysts temperature, volatile organic matter is by catalytic combustion, through adjusting superfluous heat is taken away by waste heat boiler or heat exchanger (9), the high-temp waste gas that purifies enters another reactor (12), through lower end inert filler (6) with the heat transferred filler, and savings therein, gas is lowered the temperature gradually, enter blast pipe (14) through the connected valve of giving vent to anger (4), after the half period that reaches time relay setting, the valve of opening (1) (4) is closed, the valve of closing (2) (3) is opened, reactant flows to and changes, enter another reactor (12), waste gas enters the reaction of catalyst (8) section through this reactor lower end inert filler (6), and the gas of purification is lowered the temperature after valve (3) enters escape pipe (14) through previous reactor (11) lower end inert filler.The heat major part of exothermic reaction generation all is accumulated in the reactor bed like this, superfluous heat is removed by heat exchanger, reach effective utilization of heat, even still can reach self-heating operation, the Steam Recovery utilization that can produce 1～4Mpa when comhustible component is high when therefore combustible concentration is very low in the waste gas.
Embodiment 2:
Acrylonitrile absorbing tower exhaust gas flow direction conversion catalytic combustion equipment and technological process are preheated to catalyst and two ends inert filler more than the catalyst activity temperature (330 ℃) with embodiment 1, and tail gas combustible concentration is 10720mg/m
3, the flow-reversal cycle is 3000s, reaction velocity is 20000h
-1
Adopt a kind of load P d metallic catalyst, the simulation tail gas from absorption tower of acrylonitrile installation consists of propane, propylene and carbon monoxide total concentration 500ppm (propane: propylene: carbon monoxide=21: 7: 72 (volume ratio)), acrylonitrile concentration 52ppm, flow-reversal cycle 400s, air speed is 4000h
-1Handling back waste gas NMHC clearance reaches more than 98%.The carbon monoxide removal rate reaches more than 98%, and the acrylon clearance reaches more than 99%.
Embodiment 3:
Employing is with catalyst and equipment and the technology of embodiment 1, carbon monoxide=21: 7: 72 (volume ratio)) and the concentration 104ppm of acrylonitrile simulation acrylonitrile tail gas consists of propane, propylene and carbon monoxide total concentration 1400ppm (propane: propylene:, flow-reversal cycle 1200s, air speed is 8000h
-1The NMHC clearance reaches more than 98% in the waste gas of processing back.The carbon monoxide removal rate reaches more than 98%, and the acrylonitrile clearance reaches more than 99%.
Embodiment 4:
Equipment and technology are with embodiment 1, carbon monoxide=21: 7: 72 (volume ratio)) and acrylonitrile concentration 104ppm simulation acrylonitrile tail gas consists of propane, propylene and carbon monoxide total concentration 2400ppm (propane: propylene:, flow-reversal cycle 2000s, air speed is 15000h
-1The NMHC clearance reaches 97.5% in the waste gas of processing back.The carbon monoxide removal rate has reached more than 99%, and the acrylonitrile clearance has reached more than 99%.
Experimental example 5:
Equipment and technology are with embodiment 1, carbon monoxide=70.3: 7.8: 21.9 (volume ratio)) and acrylonitrile concentration 76ppm simulation acrylonitrile tail gas consists of propane, propylene and carbon monoxide total concentration 10870ppm, and (propane: propylene:, this forms with acrylonitrile commercial plant tail gas composition very approaching.Room temperature air inlet, air speed 7000h
-1, the flow-reversal cycle is 2400s, the NMHC clearance reaches 99% in the waste gas of processing back.The carbon monoxide removal rate reaches more than 99%, and the acrylonitrile clearance reaches more than 99%.
From the foregoing description as can be seen, adopt the effect of this technology governance tail gas from absorption tower of acrylonitrile installation fine, the waste gas after the improvement has reached discharging standards.
Claims (2)
1. administer the equipment that tail gas from absorption tower of acrylonitrile installation pollutes for one kind, it is characterized in that:
Include two groups of pneumatic or electrically operated valves of control periodically automatically in the increase of tail gas from absorption tower of acrylonitrile installation position, two fixed bed reactors, the exhaust gas processing device of the flow-reversal catalytic combustion equipment that waste heat boiler or heat exchanger constitute, in the middle of two fixed bed reactors is catalyst layer, two ends are the high heat capacity inert filler, by an air intake valve and the valve of giving vent to anger be one group two groups periodically automatically pneumatic the or electrically operated valve of control be connected with the fixed bed reactors bottom respectively, two reactor upper ends are connected with high temperature heat collector waste heat boiler or heat exchanger respectively, tail gas enters pipe and is connected with two groups of automatic control air intake valves pneumatic or electrically operated valve respectively, and the purified gas outlet is connected with two groups of automatic control valves of giving vent to anger pneumatic or electrically operated valve respectively; Catalyst is for adopting γ-Al
2O
3Being carrier, is main active ingredient with precious metals pt, Pd, is prepared from granularity with the equally distributed method of high dispersive rate: Φ 3-10mm, compression strength: 〉=50N/ grain, bulk density: 0.55-0.95Kg/L, specific surface :～250m
2The catalyst of/g; Filler can be selected regular ceramic packing for use, and bed voidage is 60～70%, the big 300～400m2/m of specific area
3, weight accumulation is 500～950kgf/m
3, or porcelain ring, porcelain ball, spalling resistance (℃)＞500, filler and catalyst amount in the reactor are by volume: upper strata filler: catalyst: lower floor's filler=0.1～0.2: 1: 2～6.
2. administer the method that tail gas from absorption tower of acrylonitrile installation pollutes for one kind, it is characterized in that: the commutation cycle that application rights requires 1 described equipment reaction thing to set by the time relay alternately enters the reactor two ends from two intake valves, when the air intake valve of a reactor is opened, its valve closing of giving vent to anger, and the air intake valve of another reactor is closed, its air outlet valve is opened, gas enters the reactor of its connection from the valve of opening, at first through the inert filler of reactor lower end by heat temperature raising gradually, near the top catalyst time, reach the activity of such catalysts temperature, volatile organic matter is by catalytic combustion, through adjusting superfluous heat is taken away by waste heat boiler or heat exchanger, the high-temp waste gas that purifies enters another reactor, through the lower end inert filler with the heat transferred filler, and savings therein, gas is lowered the temperature gradually, enter blast pipe through the connected valve of giving vent to anger, after the half period that reaches time relay setting, the valve closing of opening, the valve opening of closing, reactant flows to and changes, enter another reactor, waste gas enters the catalyst section reaction through this reactor lower end inert filler, and the gas of purification is lowered the temperature after valve enters blast pipe through previous reactor lower end inert filler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006101128347A CN101138699A (en) | 2006-09-05 | 2006-09-05 | Method and equipment for treating tail gas pollution of absorption tower of acrylonitrile device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006101128347A CN101138699A (en) | 2006-09-05 | 2006-09-05 | Method and equipment for treating tail gas pollution of absorption tower of acrylonitrile device |
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| Publication Number | Publication Date |
|---|---|
| CN101138699A true CN101138699A (en) | 2008-03-12 |
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ID=39190904
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2006101128347A Pending CN101138699A (en) | 2006-09-05 | 2006-09-05 | Method and equipment for treating tail gas pollution of absorption tower of acrylonitrile device |
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| CN (1) | CN101138699A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104772038A (en) * | 2015-03-25 | 2015-07-15 | 中国石油天然气股份有限公司 | Using Pd-CeO2Method for purifying tail gas of absorption tower of acrylonitrile device by using/Me-beta molecular sieve |
| CN104772037A (en) * | 2015-03-25 | 2015-07-15 | 中国石油天然气股份有限公司 | Using Pd-CeO2Method for purifying tail gas of absorption tower of acrylonitrile device by using Me-SAPO molecular sieve |
| CN109569272A (en) * | 2017-09-28 | 2019-04-05 | 中国石油化工股份有限公司 | HCN-containing gases processing method |
| CN110639500A (en) * | 2018-06-27 | 2020-01-03 | 中国石油化工股份有限公司 | Combustion catalyst for cyanogen-containing waste gas and application of combustion catalyst in cyanogen-containing waste gas treatment |
| CN112275127A (en) * | 2020-10-12 | 2021-01-29 | 阳江职业技术学院 | Method for purifying volatile organic pollutants in environment-friendly air |
-
2006
- 2006-09-05 CN CNA2006101128347A patent/CN101138699A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104772038A (en) * | 2015-03-25 | 2015-07-15 | 中国石油天然气股份有限公司 | Using Pd-CeO2Method for purifying tail gas of absorption tower of acrylonitrile device by using/Me-beta molecular sieve |
| CN104772037A (en) * | 2015-03-25 | 2015-07-15 | 中国石油天然气股份有限公司 | Using Pd-CeO2Method for purifying tail gas of absorption tower of acrylonitrile device by using Me-SAPO molecular sieve |
| CN109569272A (en) * | 2017-09-28 | 2019-04-05 | 中国石油化工股份有限公司 | HCN-containing gases processing method |
| CN109569272B (en) * | 2017-09-28 | 2021-11-30 | 中国石油化工股份有限公司 | Cyanogen-containing waste gas treatment method |
| CN110639500A (en) * | 2018-06-27 | 2020-01-03 | 中国石油化工股份有限公司 | Combustion catalyst for cyanogen-containing waste gas and application of combustion catalyst in cyanogen-containing waste gas treatment |
| CN112275127A (en) * | 2020-10-12 | 2021-01-29 | 阳江职业技术学院 | Method for purifying volatile organic pollutants in environment-friendly air |
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