CN104436980B - The method and apparatus processing volatile organic compound from waste gas - Google Patents
The method and apparatus processing volatile organic compound from waste gas Download PDFInfo
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Abstract
The invention provides the method and apparatus processing volatile organic compound from waste gas.The method integrated utilization compresses the process of direct-cooled absorption, may be used for processing the waste gas of the VOC of multiple concentration.In direct-cooled condensation process, the method uses the straight touch degree of depth chiller that gas-liquid directly contacts, and uses cooling waste liquid as refrigerant liquid, has saved cost, has improve efficiency.
Description
Technical field
The present invention relates to the exhaust-gas treatment of VOC (Volatile Organic Compounds, VOCs)
Field, in particular it relates to a kind of method and apparatus processing volatile organic compound from waste gas.
Background technology
VOC (VOCs) is the air pollutants that a class is important, it is common that refer to atmospheric boiling point 50～
260 DEG C, its be mainly composed of the lower boiling organic compounds such as aliphatic hydrocarbon, halogenated hydrocarbons, aromatic hydrocarbon, polycyclic aromatic hydrocarbon, alcohol, aldehyde, acid, ester
Thing
VOC major part is poisonous, and part has carcinogenecity, and part is susceptible to photochemical reaction and product
Third contact of a total solar or lunar eclipse chemical fumes, also have damages the ozone layer.Just because of the above-mentioned harm of VOCs, each state is all constantly limited by legislation
The discharge capacity of VOCs.Such as " the Cleaning Air method " of U.S.'s formulation in 1970, nineteen ninety is revised again.Japan's legislation in 1996
Limit the discharge of 53 kinds of VOCs, the discharge limiting 149 kinds of VOCs in 2002.China's discharge standard of air pollutants
(GB16297-1996) 14 class VOCs the highest permission concentration of emission, the highest permission rate of discharge are specified.
Due to the effumability of VOCs, complicated component, give and bring the biggest difficulty on processing.The method processing VOCs at present
Mainly having: absorption method, the main VOCs waste gas processing low concentration, operating cost is higher, and treating capacity is limited, and adsorbent reactivation becomes
This height；, there is burning insufficient or because of sulfur-bearing in former waste gas etc. in combustion method, directly burning, heat storage type combustion, catalysis burning etc.
And cause secondary pollution problem, and VOCs exhaust gas concentration can not be too high, and equipment, catalyst are more expensive；Corona method, is at a kind of
The low cost of reason low concentration pollutant controls technology, due to the stability of reactor long-time operation and the aspect such as catalytic efficiency is low
Reason, the method has not been achievable actual application and commercialization at present；Condensation method, be by cooling make part composition supersaturation and
Being condensed into liquid, single condensation method has bigger restriction to VOCs composition, and is extremely difficult to atmospheric emission standard.
Therefore, for the method and apparatus that can process the VOCs waste gas of various concentration, there are still demand.
Summary of the invention
The present invention combines all restrictions present on the domestic and international urgent needs for VOCs exhaust-gas treatment and technology, opens
Send out a set of process route for processing variable concentrations VOCs waste gas, it is achieved that different component, the VOCs waste gas of variable concentrations
Qualified discharge, there is preferable economic benefit and environmental benefit.Specifically, the invention provides a kind of utilize compression-direct-cooled-
The integrated approach of cryogenic absorption Regeneration Treatment variable concentrations VOCs waste gas, is particularly suited for processing complex component, variable concentrations
VOCs waste gas.
In one aspect, the invention provides a kind of method processing volatile organic compound from waste gas, the method includes
Following steps:
(a) by pending described volatile organic compound from waste gas ingress pipe shell heat exchanger, with cryogen heat exchange
And lower the temperature, obtain the waste gas after pre-cooling；
(b) will derive from the waste gas after the described pre-cooling of step (a) import straight touch degree of depth chiller, by be imported into
The refrigeration liquid stream direct contact heat transfer of described straight touch degree of depth chiller is lowered the temperature, and cools down in the described straight touch degree of depth subsequently
Device carries out gas-liquid separation, goes out oral fluid producing straight touch degree of depth chiller exit flow and straight touch degree of depth chiller
Stream, wherein, a part for described straight touch degree of depth chiller outlet liquid stream is collected as waste liquid, and another part is through deep cooling
After device cools down further, it is imported into described straight touch degree of depth chiller as described refrigeration liquid stream；
C () will derive from the described direct-cooled segregation apparatus exit flow of step (b) as the cryogen described in step (a)
Heated up with described pending VOC heat exchange by described shell-and-tube heat exchanger, be subsequently sent to High Pressure Absorption
Device adsorbs, and obtains the waste gas processed through High Pressure Absorption, wherein, after absorption is saturated, carries out High Pressure Absorption device
Desorption and regeneration, and the gas desorbed is passed to the pending described volatile organic compound from waste gas described in step (a)
In；
D () will derive from the described waste gas through High Pressure Absorption process of step (c) after granular active carbon purifying, it is thus achieved that
Aerofluxus up to standard.
Preferably, in step (a), described pending waste gas is entered gas compressor by aerator, compressed
The described shell-and-tube heat exchanger of rear importing.
Preferably, the outlet pressure of described aerator is 0.1 to 0.15MPa, and the outlet pressure of described gas compressor is
0.5 to 2MPa, temperature is 30 to 75 DEG C.
Preferably, in step (b), the temperature of the waste gas after described pre-cooling is-20 to 22.5 DEG C, pressure be 0.5 to
2MPa。
Preferably, in step (c), described direct-cooled segregation apparatus exit flow is before entering described shell-and-tube heat exchanger
Temperature is-80 to-10 DEG C, and pressure is 0.5 to 2MPa, and is-25 to 17.5 DEG C by the temperature after described shell-and-tube heat exchanger,
Pressure is 0.5 to 2MPa.
Preferably, in the High Pressure Absorption device described in step (c), at temperature and 0.5 to the 2MPa of-25 to 17.5 DEG C
Pressure under, carry out described High Pressure Absorption process；And by decompression, in the temperature of 20 to 70 DEG C and the pressure of 0.1 to 0.15MPa
Under power, carry out described desorption and regeneration.
Preferably, at least two High Pressure Absorption device is used to realize the continuous processing of gas by rotation in step (c).
In yet another aspect, the invention provides a kind of equipment processing volatile organic compound from waste gas, equipment includes
Three below part:
Pre-cooling portion, described pre-cooling portion comprises aerator C1, gas compressor C2 and shell-and-tube heat exchanger F1, wherein, volatilization
Property organic compound from waste gas admission line 1 is fluidly coupled to the entrance of aerator C1, and the outlet of aerator C1 is fluidly coupled to gas
The entrance of gas compressor C2, the outlet of gas compressor C2 is fluidly coupled to the tube side import of shell-and-tube heat exchanger F1；
Straight touch degree of depth cooling end, described straight touch degree of depth cooling end comprises straight touch degree of depth chiller T1, deep cooling dress
Putting F2 and waste collecting device V1, wherein, the tube side outlet of shell-and-tube heat exchanger F1 is fluidly coupled to direct-cooled segregation apparatus T1's
Gas phase entrance, direct-cooled segregation apparatus T1 also has liquid phase entrance, gaseous phase outlet and liquid-phase outlet, and described liquid-phase outlet passes through pipeline
7 material inlets being fluidly coupled to cryogenic system F2, the material outlet of cryogenic system F2 is fluidly coupled to the cooling of the straight touch degree of depth
The liquid phase entrance of device T1, pipeline 7 has the take-off line 8 fluidly connected with waste collecting device V1, direct-cooled segregation apparatus T1
Gaseous phase outlet be fluidly coupled to the shell side inlet of shell-and-tube heat exchanger F1；
Adsorption section, described adsorption section comprises High Pressure Absorption device P1 to Pn and granular active carbon adsorbent equipment GAC, wherein, n
For the integer not less than 2, the shell-side outlet of shell-and-tube heat exchanger F1 is connected to the entrance of High Pressure Absorption device P1 to Pn, and high pressure is inhaled
The outlet of adsorption device P1 to Pn fluidly connects respectively with admission line 1 and granular active carbon adsorbent equipment GAC.
Compared with prior art, the invention have the advantages that
The method integration of the present invention condensation method and absorption method, can process complex component, variable concentrations VOCs waste gas, especially
It is applicable to the waste gas processing VOCs concentration higher than 500ppm.Especially, present invention employs straight touch degree of depth chiller.With
Gas phase heat-exchanging process compares, and straight touch degree of depth cooling tower systems uses liquid phase direct contact heat transfer technique.As one example,
Liquid distribution device, gas-liquid heat exchange filler and gas distributor it is disposed with from top to bottom in straight touch degree of depth cooling tower；Deeply
Despumation device is set on the upside of cold tower, gas to be cooled from the bottom of tower enter and with liquid countercurrent contact heat-exchanging.By using straight touch
Waste gas and the direct gas-to-liquid contact of refrigerant liquid are carried out heat exchange condensation separation by degree of depth chiller, and heat exchanger can be greatly lowered
Heat exchange area, saves equipment investment；And by a part for condensed waste gas be used as above-mentioned refrigerant liquid, simplify operation and
Installation cost, reduces energy expenditure.And, the outlet cooling gas of straight touch degree of depth cooling tower is used for the pre-of inlet gas
Cold, air cooling system can be substituted with precooler, straight touch degree of depth cooling tower exit gas cold can be reclaimed again, moreover it is possible to by this outlet
Gas regulation, to the temperature of suitable absorption, decreases condensation and the running cost of absorption, thus improves process VOCs waste gas economy
Benefit.
Additionally, present invention process device therefor assembles flexibly, it is adaptable to many occasions, the VOCs exhaust-gas treatment of multi-state.Make
By the scope of the pressure and temperature condition obtained through inventor's research, can the VOCs waste gas of various complex components be carried out up to standard
Process.
Accompanying drawing explanation
Accompanying drawing 1 is the process route view for the treatment of in accordance with the present invention VOCs waste gas.Wherein schematically illustrate two
Individual adsorption tanks P1 and P2.But it is equally useful more than two adsorption tanks.
The most each symbol represents:
C1: aerator；C2: gas compressor；F1: shell-and-tube heat exchanger (precooler)；T1 straight touch degree of depth chiller；
F2: cryogenic system；S1: refrigeration machine；P1: High Pressure Absorption tank 1；P2: High Pressure Absorption tank 2；GAC: absorbent charcoal adsorption tank；V1: waste liquid
Collecting tank.
1:VOCs waste gas；2: gas compressor inlet stream；3: gas compressor outlet streams；4: straight touch degree of depth cooling
Tower gas phase inlet stream；5: straight touch degree of depth cooling tower gaseous phase outlet logistics；6: precooler shell-side outlet logistics；7: straight touch is deep
Degree cooling tower liquid phase exit stream；8: straight touch degree of depth cooling tower liquid phase extraction logistics；9: straight touch degree of depth cooling tower liquid phase is entered
Mouth logistics；10: refrigeration machine outlet streams；11: the backflow of refrigeration machine；12: cryogenic high pressure adsorption tanks 1 inlet stream；13: low temperature is high
Pressure adsorption tanks 2 inlet stream；14: cryogenic high pressure adsorption tanks 1 outlet streams；15: cryogenic high pressure adsorption tanks 2 outlet streams；16: high
Concentration desorbing waste gas；17:GAC inlet stream；18:GAC outlet streams.
Detailed description of the invention
Detailed description below apparatus and method of the present invention.
Apparatus and method of the present invention is used for processing volatile organic compound from waste gas.Common VOCs is shown in Table 1.
The VOCs that table 1 is common
Table 2 lists the highest permission concentration of emission of (GB16297-1996) 12 kinds of organic pollutions.
The highest permission concentration of emission of table 2 some organic pollutants
| Organic substance title | The highest permission concentration of emission mg/m3 |
| Benzene | 17 |
| Toluene | 60 |
| Dimethylbenzene | 90 |
| Phenols | 115 |
| Formaldehyde | 30 |
| Acetaldehyde | 150 |
| Acrylonitrile | 26 |
| Acrylic aldehyde | 20 |
| Methanol | 220 |
| Phenyl amines | 25 |
| Chlorobenzene class | 85 |
| Vinyl chloride | 65 |
In one embodiment, the device of the process VOCs waste gas that the present invention provides includes:
Pre-cooling portion, including: aerator C1；Gas compressor C2；Shell-and-tube heat exchanger F1；
Straight touch degree of depth cooling end: straight touch degree of depth cooling tower, T1；Cryogenic system F2；Refrigeration machine S1；Waste collecting device
V1；
Adsorption section: High Pressure Absorption tank P1, P2；Absorbent charcoal adsorption tank, GAC.
It is configured to: VOCs waste gas is connected by pipeline with aerator C1 import, aerator C1 outlet and gas compressor
C2 entrance is connected by pipeline, and gas compressor C2 outlet is connected by pipeline with shell-and-tube heat exchanger F1 tube side import.Shell
The outlet of formula heat exchanger F1 tube side is connected with the gas phase entrance of straight touch degree of depth cooling tower T1, the gas phase of straight touch degree of depth cooling tower T1
Outlet is connected with the shell side import of shell-and-tube heat exchanger F1, and shell-and-tube heat exchanger F1 shell-side outlet enters with High Pressure Absorption tank P1, P2
Mouth is connected by pipeline, and the liquid-phase outlet of straight touch degree of depth cooling tower T1 is connected with the tube side import of cryogenic system F2, and arranges
Extraction mouth is connected with waste liquid tank V1 import, and the tube side outlet of cryogenic system F2 is entered with the liquid phase of straight touch degree of depth chiller T1
Mouth is connected, and the liquid-phase outlet of refrigeration machine S1 is connected with the shell side import of cryogenic system F2, cryogenic system F2 shell-side outlet and refrigeration
The liquid-phase reflux mouth of machine S1 is connected, cryogenic high pressure adsorption tanks P1, P2 outlet by pipeline respectively with import and the work of aerator C1
Property charcoal adsorption tanks GAC be connected.
In one embodiment, the present invention processes the process route of VOCs waste gas and mainly comprises the steps that
(1) VOCs waste gas 1 enters into gas compressor C2 by aerator C1, and the outlet pressure of described aerator C1 is
0.1～0.15MPa (absolute pressure appears below force value and is absolute pressure), gas compressor C2 outlet pressure is 0.5～2MPa, temperature
Degree is 30～75 DEG C.
(2) gas compressor outlet streams 3 cools to-20～22.5 DEG C by precooler (i.e. shell-and-tube heat exchanger) F1,
Enter straight touch degree of depth cooling tower T1 after cooling and carry out deep cooling and gas-liquid separation；Bottom straight touch degree of depth cooling tower T1, refrigeration
The organic mixture of VOCs liquid phase after liquid stream and cooling is partly into cryogenic system F2, and another part accumulates a period of time
Rear extraction, extraction liquid enters waste collection tank V1, and described straight touch degree of depth cooling tower uses gas-to-liquid contact direct heat transfer, gas
Phase inlet stream 4 temperature is-20～22.5 DEG C, and pressure is 0.5～2MPa.
(3) straight touch degree of depth cooling tower gaseous phase outlet logistics 5 carries out heat exchange by precooler F1, enters high pressure and inhale after heat exchange
Attached system processes, and described straight touch degree of depth cooling tower gaseous phase outlet logistics 5 temperature is-10 DEG C～-80 DEG C, and pressure is
0.5～2MPa；Precooler shell-side outlet logistics 6 temperature is-25～17.5 DEG C, and pressure is 0.5～2MPa.
(4) cryogenic absorption regenerative system is cryogenic high pressure adsorption tanks P1 and cryogenic high pressure adsorption tanks P2 checker pressure is real
Now adsorb parsing.GAC inlet stream 17 after cryogenic high pressure absorption reaches atmospheric emission standard by absorbent charcoal adsorption tank GAC and arranges
Enter air.The adsorption process pressure of described cryogenic high pressure absorption is 0.5～2MPa, and temperature is-25 DEG C～17.5 DEG C；Described
The desorption process pressure of cryogenic high pressure absorption is 0.1～0.15MPa, and temperature is 25～70 DEG C, and cryogenic absorption regenerative system resolves
High-concentration waste gas 16 enter into aerator C1 import circular treatment by pipeline.
In other words, the waste gas containing the different VOCs of multiple boiling point through pre-cooling, in straight touch degree of depth chiller with
Refrigeration liquid stream direct contact heat transfer and lower the temperature, wherein most VOCs condense, with refrigeration liquid stream cold together as the straight touch degree of depth
Radiator cooler outlet liquid stream flows out.This outlet liquid stream part as waste collection, another part cool down once again after again as system
Cold liquid stream enters straight touch degree of depth chiller, is re-used for condensation.After eliminating a part of VOCs, in waste gas, VOCs is dense
Spending the most decreased, it leaves from straight touch degree of depth chiller gaseous phase outlet, and is used by its cold by shell-and-tube heat exchanger
In making initial exhaust gas pre-cooling before entering condensing steps.The waste gas of this low VOCs concentration enters cryogenic high pressure adsorption tanks subsequently, logical
Cross adsorption cleaning, and become air up to standard finally by after GAC absorption.And adsorbed VOCs weight during desorption and regeneration
Newly return to waste gas charging is processed again.The method of the present invention uses the integrated approach of condensation-absorption, therefore can process
The VOCs waste gas of various concentration.Especially, present invention employs straight touch degree of depth chiller, carried out by direct gas-to-liquid contact
Heat exchange condenses, and the heat exchange area of heat exchanger is greatly lowered compared with gas phase heat exchange method, saves equipment investment.And, the present invention
The exit gas of the cooling of straight touch degree of depth chiller is used for the pre-cooling of inlet exhaust gases stream, eliminates air cooling system, can return
Receive the cold of straight touch degree of depth chiller exit gas, simultaneously by the regulation of this exit gas to the temperature of suitable absorption, reduce
Condensation and the running cost of absorption, thus improve process VOCs waste gas economic benefit.
In the present invention, term " straight touch degree of depth chiller ", or more specifically, " straight touch degree of depth cooling tower ", be
Gas-liquid can be made directly to contact and by the device of VOCs waste gas condensation.Preferably, it is the device with following structure: this straight touch
Liquid distribution device, gas-liquid heat exchange filler and gas distributor it is disposed with from top to bottom in degree of depth cooling tower；Straight touch is deep
Arranging Despumation device on the upside of degree cooling tower, straight touch degree of depth cooling tower bottom outlet connects circulating pump by pipeline, and circulation pumps out
Mouth connects the arrival end of liquid-liquid heat exchanger by pipeline, and liquid distribution device is connected by the port of export of pipeline with liquid-liquid heat exchanger
Connect.
Below by concrete case study on implementation, the present invention is further detailed.
Embodiment 1-contaminated soil gas phase extracting VOCs exhaust-gas treatment:
In the present embodiment, the VOCs waste gas 1 (500NM of certain oil-polluted soils gas phase extracting is processed3/ hr), it passes through
Detection total concentration is up to 25100ppm.By aerator C1, VOCs waste gas 1 is entered gas compressor C2, and the outlet pressure of C2 is
1MPa, temperature is 50 DEG C；Gas compressor outlet streams 3 enters the cooling of the straight touch degree of depth after cooling to 5 DEG C by precooler F1
Tower T1, straight touch degree of depth cooling tower T1 pressure is 1MPa, and straight touch degree of depth cooling tower fluid inlet logistics 9 is the startup of-45 DEG C
Cold-producing medium (refrigeration liquid stream), in bottom, starts the part in the tower bottom liquid phase Organic substance produced after cold-producing medium contacts with VOCs
Entering waste collection tank V1, reserved a part of waste liquid enters chiller F2 and is cooled to-45 DEG C as above-mentioned startup cold-producing medium.
Straight touch degree of depth cooling tower gaseous phase outlet logistics 5 temperature is-40 DEG C, enters cryogenic absorption by precooler F1 heat exchange after 0 DEG C
Regenerative system processes.Waste gas after cryogenic high pressure absorption reaches atmospheric emission standard by absorbent charcoal adsorption tank GAC and enters
Air.The adsorption process pressure of cryogenic high pressure absorption is 1MPa, and temperature is 0 DEG C, and desorption process pressure is 0.1MPa, and temperature is 25
DEG C, the high-concentration waste gas 16 of cryogenic absorption regenerative system desorbing enters into aerator C1 import circular treatment by pipeline.Table 3 is
Certain contaminated soil gas phase extracting VOCs waste gas composition before treatment after contrast.
Gas composition after certain contaminated soil gas phase of table 3 extracting VOCs waste gas composition and process
Drop to 299ppm by the VOC exhaust gas concentration of the step high concentrations such as compression-direct-cooled-High Pressure Absorption, contrast GB
(GB16297-1996) related component has reached waste gas emission standard, and the method effectively achieves high concentration, complex component
The process of VOCs waste gas.
Embodiment 2-oil plant discharge VOCs exhaust-gas treatment:
In the present embodiment, certain oil plant discharge VOCs waste gas 1 (1000NM is processed3/ hr), it is high through detection total concentration
Reach 15100ppm.By aerator C1, VOCs waste gas 1 is entered gas compressor C2, and the outlet pressure of C2 is 2MPa, and temperature is
75℃；Gas compressor outlet streams 3 enters straight touch degree of depth cooling tower T1, straight touch after cooling to 0 DEG C by precooler F1
Degree of depth cooling tower T1 pressure is 2MPa, and straight touch degree of depth cooling tower fluid inlet logistics 9 uses the startup cold-producing medium (system of-85 DEG C
Cold liquid stream), in bottom, the waste liquid that is partly into started in the tower bottom liquid phase Organic substance produced after cold-producing medium contacts with VOCs is received
Collection tank V1, reserved a part of waste liquid enters chiller F2 and is cooled to-85 DEG C as above-mentioned startup cold-producing medium.The straight touch degree of depth
Cooling tower gaseous phase outlet logistics 5 temperature is-80 DEG C, enters by entering cryogenic absorption regenerative system after precooler F1 heat exchange extremely-5 DEG C
Row processes.Waste gas after cryogenic high pressure absorption reaches atmospheric emission standard by absorbent charcoal adsorption tank GAC and enters air.Low temperature is high
The adsorption process pressure of pressure absorption is 2MPa, and temperature is-5 DEG C, and desorption process pressure is 0.15MPa, and temperature is 70 DEG C, and low temperature is inhaled
The high-concentration waste gas 16 that attached regenerative system resolves enters into aerator C1 import circular treatment by pipeline.Table 4 is certain oil plant
Discharge VOCs waste gas composition contrasts before and after processing.
Gas composition after certain oil plant of table 4 discharge VOCs waste gas composition and process
The VOCs exhaust gas concentration of the high concentration processed by compression-direct-cooled-High Pressure Absorption etc. drops to 204ppm, contrasts GB
(GB16297-1996) related component has reached waste gas emission standard, and the method effectively achieves high concentration, complex component
The process of VOCs waste gas.
Embodiment 3-printing enterprise discharge VOCs exhaust-gas treatment:
In the present embodiment, certain printing enterprise discharge VOCs waste gas 1 (1000NM is processed3/ hr), high through detection total concentration
Reaching 26600ppm, by aerator C1, VOCs waste gas 1 is entered gas compressor C2, the outlet pressure of C2 is 0.5MPa, temperature
It it is 30 DEG C；Gas compressor outlet streams 3 enters straight touch degree of depth cooling tower T1 after cooling to 22.5 DEG C by precooler F1, directly
Touch degree of depth cooling tower T1 pressure is 0.5MPa, and straight touch degree of depth cooling tower fluid inlet logistics 9 is the startup cold-producing medium of-20 DEG C
(refrigeration liquid stream), in bottom, being partly in the tower bottom liquid phase Organic substance that startup cold-producing medium produces after contacting with VOCs is useless
Liquid collecting tank V1, reserved a part of waste liquid enters chiller F2 and is cooled to-20 DEG C as above-mentioned startup cold-producing medium.Straight touch
Degree of depth cooling tower gaseous phase outlet logistics 5 temperature is-10 DEG C, enters High Pressure Absorption system by precooler F1 heat exchange after-2.5 DEG C
Process.Waste gas after cryogenic high pressure absorption reaches atmospheric emission standard by absorbent charcoal adsorption tank GAC and enters air.Low temperature
The adsorption process pressure of High Pressure Absorption is 0.5MPa, and temperature is-2.5 DEG C, and desorption process pressure is 0.12MPa, and temperature is 40 DEG C,
The high-concentration waste gas 16 of cryogenic absorption regenerative system desorbing enters into aerator C1 import circular treatment by pipeline.Table 5 is certain
Printing enterprise's discharge VOCs waste gas composition contrasts before and after processing.
Gas composition after certain printing enterprise of table 5 discharge VOCs waste gas composition and process
The VOCs exhaust gas concentration of the high concentration processed by compression-direct-cooled-High Pressure Absorption etc. drops to 305PPM, contrasts GB
(GB16297-1996) related component has reached waste gas emission standard, and the method effectively achieves high concentration, complex component
The process of VOCs waste gas.
Embodiment 4-coatings enterprises discharge VOCs exhaust-gas treatment:
In the present embodiment, certain coatings enterprises discharge VOCs waste gas 1 (500NM is processed3/ hr), high through detection total concentration
Reaching 26900ppm, by aerator C1, VOCs waste gas 1 is entered gas compressor C2, the outlet pressure of C2 is 0.6MPa, temperature
It it is 35 DEG C；Gas compressor outlet streams 3 enters straight touch degree of depth cooling tower T1 after cooling to 5 DEG C by precooler F1, directly touch
Formula degree of depth cooling tower T1 pressure is 0.6MPa, straight touch degree of depth cooling tower fluid inlet logistics 9 use-50 DEG C startup refrigeration
Agent (refrigeration liquid stream), in bottom, starts being partly in the tower bottom liquid phase Organic substance produced after cold-producing medium contacts with VOCs
Waste collection tank V1, reserved a part of waste liquid enters chiller F2 and is cooled to-50 DEG C as above-mentioned startup cold-producing medium.Straight tactile
Formula degree of depth cooling tower gaseous phase outlet logistics 5 temperature is-45 DEG C, enters cryogenic absorption regeneration by precooler F1 heat exchange after-5 DEG C
System processes.Waste gas after cryogenic absorption regeneration reaches atmospheric emission standard by absorbent charcoal adsorption tank GAC and enters air.
The adsorption process pressure of High Pressure Absorption is 0.6MPa, and temperature is-5 DEG C, and desorption process pressure is 0.14MPa, and temperature is 55 DEG C, low
The high-concentration waste gas 16 of temperature absorption regeneration system desorbing enters into aerator C1 import circular treatment by pipeline.Table 6 is that certain is coated with
Material enterprise discharge VOCs waste gas composition contrasts before and after processing.
Gas composition after certain coatings enterprises of table 6 discharge VOCs waste gas composition and process
The VOCs exhaust gas concentration of the high concentration processed by compression-direct-cooled-High Pressure Absorption etc. drops to 375PPM, contrasts GB
(GB16297-1996) related component has reached waste gas emission standard, and the method effectively achieves high concentration, complex component
The process of VOCs waste gas.
A kind of process processing VOCs waste gas that the present invention proposes, is described by preferred embodiment, phase
Close technical staff substantially in without departing from present invention, spirit and scope, structure as herein described and technical method to be carried out
Change or suitably change and combination, realize the technology of the present invention.Special needs to be pointed out is, all similar replacements and change
Apparent to those skilled in the art, they are considered as being included in present invention spirit, scope and content.
Claims (8)
1. the method processing volatile organic compound from waste gas, said method comprising the steps of:
A (), by pending described volatile organic compound from waste gas ingress pipe shell heat exchanger, is dropped with cryogen heat exchange
Temperature, obtains the waste gas after pre-cooling；
B () will derive from the waste gas after the described pre-cooling of step (a) and import straight touch degree of depth chiller, by be imported into described
The refrigeration liquid stream direct contact heat transfer of straight touch degree of depth chiller is lowered the temperature, subsequently at described straight touch degree of depth chiller
In carry out gas-liquid separation, with produce straight touch degree of depth chiller exit flow and the straight touch degree of depth chiller outlet liquid stream,
Wherein, a part for described straight touch degree of depth chiller outlet liquid stream is collected as waste liquid, and another part fills through deep cooling
After putting cooling further, it is imported into described straight touch degree of depth chiller as described refrigeration liquid stream；
C () will derive from the described straight touch degree of depth chiller exit flow of step (b) as the low temperature stream described in step (a)
Body is heated up by described shell-and-tube heat exchanger and described pending VOC heat exchange, is subsequently sent to high pressure and inhales
Adsorption device adsorbs, and obtains the waste gas processed through High Pressure Absorption, wherein, after absorption is saturated, enters High Pressure Absorption device
Row desorption and regeneration, and it is useless that the gas desorbed passes to the pending described VOC described in step (a)
In gas；
D () will derive from the described waste gas through High Pressure Absorption process of step (c) after granular active carbon purifying, it is thus achieved that up to standard
Aerofluxus.
Method the most according to claim 1, wherein, in step (a), is entered described pending waste gas by aerator
Enter gas compressor, import described shell-and-tube heat exchanger after compression.
Method the most according to claim 2, wherein, the outlet pressure of described aerator is 0.1 to 0.15MPa, described gas
The outlet pressure of gas compressor is 0.5 to 2MPa, and temperature is 30 to 75 DEG C.
Method the most according to claim 1, wherein, in step (b), the temperature of the waste gas after described pre-cooling be-20 to
22.5 DEG C, pressure is 0.5 to 2MPa.
Method the most according to claim 1, wherein, in step (c), described straight touch degree of depth chiller exit flow
Temperature before entering described shell-and-tube heat exchanger is-80 to-10 DEG C, and pressure is 0.5 to 2MPa, and is changed by described shell-and-tube
Temperature after hot device is-25 to 17.5 DEG C, and pressure is 0.5 to 2MPa.
Method the most according to claim 1, wherein, in the High Pressure Absorption device described in step (c) ,-25 to
At the temperature of 17.5 DEG C and the pressure of 0.5 to 2MPa, carry out described High Pressure Absorption process；And by decompression, at 20 to 70 DEG C
Temperature and 0.1 to 0.15MPa pressure under, carry out described desorption and regeneration.
Method the most according to claim 1, wherein, uses at least two High Pressure Absorption to fill by rotation in step (c)
Put the continuous processing realizing gas.
8., for processing an equipment for volatile organic compound from waste gas, described equipment includes:
Pre-cooling portion, described pre-cooling portion comprises aerator (C1), gas compressor (C2) and shell-and-tube heat exchanger (F1), wherein, waves
The property sent out organic compound from waste gas admission line (1) is fluidly coupled to the entrance of aerator (C1), the outlet fluid of aerator (C1)
Being connected to the entrance of gas compressor (C2), the outlet of gas compressor (C2) is fluidly coupled to the pipe of shell-and-tube heat exchanger (F1)
Journey import；
Straight touch degree of depth cooling end, described straight touch degree of depth cooling end comprises straight touch degree of depth chiller (T1), cryogenic system
(F2) and waste collecting device (V1), wherein, to be fluidly coupled to the straight touch degree of depth cold in the tube side outlet of shell-and-tube heat exchanger (F1)
The gas phase entrance of radiator cooler (T1), straight touch degree of depth chiller (T1) also has liquid phase entrance, gaseous phase outlet and liquid-phase outlet,
Described liquid-phase outlet is fluidly coupled to the material inlet of cryogenic system (F2) by pipeline (7), and the material of cryogenic system (F2) goes out
Mouth is fluidly coupled to the liquid phase entrance of straight touch degree of depth chiller (T1), and pipeline (7) has and waste collecting device (V1) stream
The take-off line (8) that body connects, the gaseous phase outlet of straight touch degree of depth chiller (T1) is fluidly coupled to shell-and-tube heat exchanger
(F1) shell side inlet,
Adsorption section, described adsorption section comprises granular active carbon adsorbent equipment (GAC) and two or more High Pressure Absorption device, wherein,
The shell-side outlet of shell-and-tube heat exchanger (F1) is connected to the entrance of described High Pressure Absorption device, the outlet of described High Pressure Absorption device
Fluidly connect respectively with admission line (1) and granular active carbon adsorbent equipment (GAC).
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| CN105709559A (en) * | 2016-04-11 | 2016-06-29 | 惠州市盛和化工有限公司 | Volatile organic waste gas treatment process and treatment equipment used in treatment process |
| CN109709280A (en) * | 2019-01-21 | 2019-05-03 | 河南弘康环保科技有限公司 | A kind of detection method of quick accounting valve uncontrollable discharge volatile organic matter |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5122165A (en) * | 1990-07-10 | 1992-06-16 | International Environmental Systems, Inc. | Removal of volatile compounds and surfactants from liquid |
| CN202751933U (en) * | 2012-08-27 | 2013-02-27 | 浙江大学 | Four-section type sludge drying off-gas treatment system |
| CN103933854A (en) * | 2014-02-25 | 2014-07-23 | 中国科学院生态环境研究中心 | Fluidized bed adsorption and desorption apparatus and method of organic exhaust gas |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5122165A (en) * | 1990-07-10 | 1992-06-16 | International Environmental Systems, Inc. | Removal of volatile compounds and surfactants from liquid |
| CN202751933U (en) * | 2012-08-27 | 2013-02-27 | 浙江大学 | Four-section type sludge drying off-gas treatment system |
| CN103933854A (en) * | 2014-02-25 | 2014-07-23 | 中国科学院生态环境研究中心 | Fluidized bed adsorption and desorption apparatus and method of organic exhaust gas |
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