CN104436980A - Method and equipment for processing exhaust gases of volatile organic compounds - Google Patents
Method and equipment for processing exhaust gases of volatile organic compounds Download PDFInfo
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Abstract
The invention provides a method and equipment for processing exhaust gases of volatile organic compounds. In the method, the processes of compression-direct cooling-adsorption are integrated, and the method can be used for processing exhaust gases, with a plurality of concentrations, of the volatile organic compounds. According to the method, a direct-contact depth cooling device adopting gas-liquid direct contact is adopted in the direct cooling condensation process; and cooling liquid waste is utilized as refrigerant liquid, so that the cost is reduced, and the efficiency is improved.
Description
Technical field
The present invention relates to the exhaust-gas treatment field of VOC (Volatile Organic Compounds, VOCs), particularly, relate to a kind of method and apparatus processing volatile organic compound from waste gas.
Background technology
VOC (VOCs) is the important air pollutants of a class, typically refer to atmospheric boiling point 50 ~ 260 DEG C, its main component is aliphatic hydrocarbon, halogenated hydrocarbons, aromatic hydrocarbon, the lower boiling organic compound such as polycyclic aromatic hydrocarbon, alcohol, aldehyde, acid, ester
VOC major part is poisonous, and part has carcinogenicity, and part photochemical reaction easily occurs and produces photochemical fog, and what also have damages the ozone layer.Just because of the above-mentioned harm of VOCs, each state all passes through to make laws and constantly limits the discharge capacity of VOCs.As " the Cleaning Air method " of U.S.'s formulation in 1970, nineteen ninety revises again.The discharge of Japan's legislation restriction in 1996 53 kinds of VOCs, the discharge of restriction in 2002 149 kinds of VOCs.China's discharge standard of air pollutants (GB16297-1996) specifies 14 class VOCs the highest permission concentration of emission, the highest permission rate of discharge.
Due to the effumability of VOCs, complicated component, gives in process and brings very large difficulty.The method of current process VOCs mainly contains: absorption method, the VOCs waste gas of main process low concentration, and operating cost is higher, and treating capacity is limited, and adsorbent reactivation cost is high; Combustion method, directly burning, heat storage type combustion, catalytic combustion etc., there is burning insufficient or cause secondary pollution problem because of sulfur-bearing in former waste gas etc., and VOCs exhaust gas concentration can not be too high, and equipment, catalyst are more expensive; Corona method is a kind of low cost control technology processing low concentration pollutant, and due to the stability of reactor long-time operation and the reasons such as catalytic efficiency is low, the method also fails to realize practical application and commercialization at present; Condensation method, be make part form supersaturation by cooling and be condensed into liquid, independent condensation method has larger restriction to VOCs composition, and is difficult to reach atmospheric emission standard.
Therefore, for the method and apparatus of VOCs waste gas that can process various concentration, still there is demand.
Summary of the invention
The present invention combines both at home and abroad for the active demand of VOCs exhaust-gas treatment and all restrictions of technically existence, develop a set of process route for the treatment of variable concentrations VOCs waste gas, achieve different component, the qualified discharge of the VOCs waste gas of variable concentrations, has good economic benefit and environmental benefit.Particularly, the invention provides a kind of integrated approach utilizing compression-direct-cooled-cryogenic absorption regeneration process variable concentrations VOCs waste gas, be particularly useful 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 comprises the following steps:
A (), by pending described volatile organic compound from waste gas ingress pipe shell heat exchanger, is lowered the temperature with cryogen heat exchange, is obtained the waste gas after precooling;
B waste gas after the described precooling deriving from step (a) is imported straight touch degree of depth cooling device by (), by lowering the temperature with the refrigerating fluid stream direct contact heat transfer being imported into described straight touch degree of depth cooling device, gas-liquid separation is carried out subsequently in described straight touch degree of depth cooling device, to produce straight touch degree of depth cooling device exit flow and straight touch degree of depth cooling device goes out oral fluid stream, wherein, the part that described straight touch degree of depth cooling device goes out oral fluid stream is collected as waste liquid, another part is after cryogenic system cools further, described straight touch degree of depth cooling device is imported into as described refrigerating fluid stream,
C the described direct-cooled separator exit flow deriving from step (b) is heated up as the cryogen described in step (a) by described shell-and-tube heat exchanger and described pending VOC heat exchange by (), deliver to High Pressure Absorption device subsequently to adsorb, obtain the waste gas through High Pressure Absorption process, wherein, after absorption is saturated, desorption and regeneration is carried out to High Pressure Absorption device, and the gas separating sucking-off is passed in the pending described volatile organic compound from waste gas described in step (a);
D () will derive from the described waste gas through High Pressure Absorption process of step (c) after granular active carbon purifying, obtain exhaust up to standard.
Preferably, in step (a), described pending waste gas is entered gas compressor by air blast, import described shell-and-tube heat exchanger after compression.
Preferably, the outlet pressure of described air blast is 0.1 to 0.15MPa, and the outlet pressure of described gas compressor is 0.5 to 2MPa, and temperature is 30 to 75 DEG C.
Preferably, in step (b), the temperature of the waste gas after described precooling is-20 to 22.5 DEG C, and pressure is 0.5 to 2MPa.
Preferably, in step (c), the temperature of described direct-cooled separator exit flow before entering described shell-and-tube heat exchanger is-80 to-10 DEG C, and pressure is 0.5 to 2MPa, and be-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), under the pressure of the temperature of-25 to 17.5 DEG C and 0.5 to 2MPa, carry out described High Pressure Absorption process; And by decompression, under the pressure of the temperature of 20 to 70 DEG C and 0.1 to 0.15MPa, carry out described desorption and regeneration.
Preferably, in step (c), at least two High Pressure Absorption devices are used to realize the continuous process of gas by rotation.
In yet another aspect, the invention provides a kind of equipment processing volatile organic compound from waste gas, equipment comprises following three parts:
Precooling portion, described precooling portion comprises air blast C1, gas compressor C2 and shell-and-tube heat exchanger F1, wherein, volatile organic compound from waste gas admission line 1 fluid is connected to the entrance of air blast C1, the outlet fluid of air blast C1 is connected to the entrance of gas compressor C2, and the outlet fluid of gas compressor C2 is connected 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 cooling device T1, cryogenic system F2 and waste collecting device V1, wherein, the tube side outlet fluid of shell-and-tube heat exchanger F1 is connected to the gas phase entrance of direct-cooled separator T1, direct-cooled separator T1 also has liquid phase entrance, gaseous phase outlet and liquid-phase outlet, described liquid-phase outlet is connected to the material inlet of cryogenic system F2 by pipeline 7 fluid, the material outlet fluid of cryogenic system F2 is connected to the liquid phase entrance of straight touch degree of depth cooling device T1, pipeline 7 has the take-off line 8 be connected with waste collecting device V1 fluid, the gaseous phase outlet fluid of direct-cooled separator T1 is connected 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 be not less than 2 integer, 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 the outlet of High Pressure Absorption device P1 to Pn is connected with admission line 1 and granular active carbon adsorbent equipment GAC difference fluid.
Compared with prior art, the present invention has the following advantages:
Method integration of the present invention condensation method and absorption method, can process complex component, variable concentrations VOCs waste gas, is particularly useful for processing the waste gas of VOCs concentration higher than 500ppm.Especially, present invention employs straight touch degree of depth cooling device.Compare with gas phase heat-exchanging process, straight touch degree of depth cooling tower systems adopts liquid phase direct contact heat transfer technique.As an one example, in straight touch degree of depth cooling tower, be disposed with liquid distribution device, gas-liquid heat exchange filler and gas distributor from top to bottom; On the upside of deep cooling tower, Despumation device is set, gas to be cooled enter at the bottom of tower and with liquid countercurrent contact heat-exchanging.By adopting straight touch degree of depth cooling device that waste gas and the direct gas-liquid contact of refrigerant liquid are carried out heat exchange condensation separation, significantly can reduce the heat exchange area of heat exchanger, saving equipment investment; And a part for condensed waste gas is used as above-mentioned refrigerant liquid, simplifies operation and installation cost, reduce energy ezpenditure.And, the outlet refrigerating gas of straight touch degree of depth cooling tower is used for the precooling of inlet gas, air cooling system can be substituted with forecooler, straight touch degree of depth cooling tower exit gas cold can be reclaimed again, this exit gas can also be adjusted to the temperature of suitable absorption, decrease the running cost of condensation and absorption, thus improve process VOCs waste gas economic benefit.
In addition, the assembling of present invention process device therefor flexibly, is applicable to the VOCs exhaust-gas treatment of many occasions, multi-state.Use the scope studying the pressure and temperature condition obtained through inventor, process up to standard can be carried out to the VOCs waste gas of various complex component.
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 adsorption tanks P1 and P2.But can use equally more than two adsorption tanks.
Wherein each symbol represents:
C1: air blast; C2: gas compressor; F1: shell-and-tube heat exchanger (forecooler); T1 straight touch degree of depth cooling device; 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 collection 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: the logistics of forecooler shell-side outlet; 7: straight touch degree of depth 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 fluid inlet logistics; 10: refrigeration machine outlet streams; 11: the backflow of refrigeration machine; 12: cryogenic high pressure adsorption tanks 1 inlet stream; 13: cryogenic 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 desorb waste gas; 17:GAC inlet stream; 18:GAC outlet streams.
Detailed description of the invention
Below illustrate apparatus and method of the present invention.
Apparatus and method of the present invention are for the treatment of volatile organic compound from waste gas.Common VOCs is in table 1.
The VOCs that table 1 is common
The highest permission concentration of emission of table 2 lists (GB16297-1996) 12 kinds of organic pollutions.
The highest permission concentration of emission of table 2 some organic pollutants
| Organic matter title | The highest permission concentration of emission mg/m 3 |
| Benzene | 17 |
| Toluene | 60 |
| Dimethylbenzene | 90 |
| Phenols | 115 |
| Formaldehyde | 30 |
| Acetaldehyde | 150 |
| Acrylonitrile | 26 |
| Methacrylaldehyde | 20 |
| Methyl alcohol | 220 |
| Phenyl amines | 25 |
| Chlorobenzene class | 85 |
| Vinyl chloride | 65 |
In one embodiment, the device of process VOCs waste gas provided by the invention comprises:
Precooling portion, comprising: air blast 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 air blast C1 import, and air blast C1 outlet is connected by pipeline with gas compressor C2 entrance, and gas compressor C2 outlet is connected by pipeline with the import of shell-and-tube heat exchanger F1 tube side.The outlet of shell-and-tube heat exchanger F1 tube side is connected with the gas phase entrance of straight touch degree of depth cooling tower T1, the gaseous phase outlet of straight touch degree of depth cooling tower T1 is connected with the shell side import of shell-and-tube heat exchanger F1, shell-and-tube heat exchanger F1 shell-side outlet and High Pressure Absorption tank P1, P2 import is connected by pipeline, 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 extraction mouth is set is connected with waste liquid tank V1 import, the tube side outlet of cryogenic system F2 is connected with the fluid inlet of straight touch degree of depth cooling device T1, 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 is connected with the liquid-phase reflux mouth of refrigeration machine S1, cryogenic high pressure adsorption tanks P1, P2 outlet is connected with the import of air blast C1 and absorbent charcoal adsorption tank GAC respectively by pipeline.
In one embodiment, the process route of process VOCs waste gas of the present invention mainly comprises the following steps:
(1) VOCs waste gas 1 enters into gas compressor C2 by air blast C1, the outlet pressure of described air blast C1 is 0.1 ~ 0.15MPa (absolute pressure, below occur that force value is absolute pressure), gas compressor C2 outlet pressure is 0.5 ~ 2MPa, and temperature is 30 ~ 75 DEG C.
(2) gas compressor outlet streams 3 cools to-20 ~ 22.5 DEG C by forecooler (i.e. shell-and-tube heat exchanger) F1, enters straight touch degree of depth cooling tower T1 and carry out deep cooling and gas-liquid separation after cooling; Bottom straight touch degree of depth cooling tower T1, refrigerating fluid stream and the organic mixture part of cooled VOCs liquid phase enter cryogenic system F2, another part accumulates extraction after a period of time, extraction liquid enters waste collection tank V1, described straight touch degree of depth cooling tower adopts gas-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 forecooler F1, enter High Pressure Absorption system after heat exchange to process, 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; Forecooler shell-side outlet logistics 6 temperature is-25 ~ 17.5 DEG C, and pressure is 0.5 ~ 2MPa.
(4) cryogenic absorption regenerative system is that cryogenic high pressure adsorption tanks P1 and cryogenic high pressure adsorption tanks P2 checker pressure realize absorption parsing.GAC inlet stream 17 after cryogenic high pressure absorption reaches atmospheric emission standard by absorbent charcoal adsorption tank GAC and enters 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; The desorption process pressure of described cryogenic high pressure absorption is 0.1 ~ 0.15MPa, and temperature is 25 ~ 70 DEG C, and the high-concentration waste gas 16 that cryogenic absorption regenerative system is resolved enters into air blast C1 import circular treatment by pipeline.
In other words, waste gas containing the different VOCs of multiple boiling point is through precooling, lower the temperature with refrigerating fluid stream direct contact heat transfer in straight touch degree of depth cooling device, wherein most of VOCs condensation, goes out oral fluid stream as straight touch degree of depth cooling device and flows out together with refrigerating fluid stream.This goes out an oral fluid stream part as waste collection, again flows to into straight touch degree of depth cooling device, again for condensation as refrigerating fluid after another part cools once again.After eliminating a part of VOCs, in waste gas, VOCs concentration reduces, and it leaves from straight touch degree of depth cooling device gaseous phase outlet, and is used for making initial exhaust gas precooling before entering condensing steps by its cold by shell-and-tube heat exchanger.The waste gas of this low VOCs concentration enters cryogenic high pressure adsorption tanks subsequently, by adsorption cleaning, and becomes air up to standard finally by after GAC absorption.And come back in waste gas charging in desorption and regeneration process by the VOCs adsorbed and again processed.Method of the present invention adopts 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 cooling device, carry out heat exchange condensation by direct gas-liquid contact, significantly reduce the heat exchange area of heat exchanger compared with gas phase heat exchange method, save equipment investment.And, the exit gas of the cooling of straight touch degree of depth cooling device is used for the precooling of inlet exhaust gases stream by the present invention, eliminate air cooling system, the cold of straight touch degree of depth cooling device exit gas can be reclaimed, this exit gas is adjusted to the temperature of suitable absorption simultaneously, decrease the running cost of condensation and absorption, thus improve process VOCs waste gas economic benefit.
In the present invention, term " straight touch degree of depth cooling device ", or more specifically, " straight touch degree of depth cooling tower " gas-liquid can be made directly to contact and by the device of VOCs waste gas condensation.Preferably, be the device with following structure: in this straight touch degree of depth cooling tower, be disposed with liquid distribution device, gas-liquid heat exchange filler and gas distributor from top to bottom; On the upside of straight touch degree of depth cooling tower, Despumation device is set, straight touch degree of depth cooling tower bottom outlet connects circulating pump by pipeline, circulating-pump outlet is by the arrival end of pipeline connecting fluid-liquid heat exchanger, and liquid distribution device is connected by the port of export of pipeline with liquid-liquid heat exchanger.
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 processed
3/ hr), it is through detecting total concentration up to 25100ppm.VOCs waste gas 1 is entered gas compressor C2 by air blast C1, and the outlet pressure of C2 is 1MPa, and temperature is 50 DEG C; Gas compressor outlet streams 3 enters straight touch degree of depth cooling tower T1 after cooling to 5 DEG C by forecooler F1, straight touch degree of depth cooling tower T1 pressure is 1MPa, straight touch degree of depth cooling tower fluid inlet logistics 9 is the startup cold-producing medium (refrigerating fluid stream) of-45 DEG C, in bottom, the part started in liquid phase organic matter at the bottom of the tower produced after cold-producing medium contacts with VOCs enters waste collection tank V1, and reserved a part of waste liquid enters deep freezer 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, processes by entering cryogenic absorption regenerative system after forecooler F1 heat exchange to 0 DEG C.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, and the high-concentration waste gas 16 of cryogenic absorption regenerative system desorb enters into air blast C1 import circular treatment by pipeline.Table 3 be certain contaminated soil gas phase extracting VOCs waste gas composition before treatment after contrast.
Certain contaminated soil gas phase extracting of table 3 VOCs waste gas composition and the gas composition after processing
299ppm is dropped to 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 reaches waste gas emission standard, and the method effectively achieves the process of high concentration, complex component 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 processed
3/ hr), it is through detecting total concentration up to 15100ppm.VOCs waste gas 1 is entered gas compressor C2 by air blast C1, and the outlet pressure of C2 is 2MPa, and temperature is 75 DEG C; Gas compressor outlet streams 3 enters straight touch degree of depth cooling tower T1 after cooling to 0 DEG C by forecooler F1, straight touch degree of depth cooling tower T1 pressure is 2MPa, straight touch degree of depth cooling tower fluid inlet logistics 9 adopts the startup cold-producing medium (refrigerating fluid stream) of-85 DEG C, in bottom, the part started in liquid phase organic matter at the bottom of the tower produced after cold-producing medium contacts with VOCs enters waste collection tank V1, and reserved a part of waste liquid enters deep freezer F2 and is cooled to-85 DEG C as above-mentioned startup cold-producing medium.Straight touch degree of depth cooling tower gaseous phase outlet logistics 5 temperature is-80 DEG C, processes by entering cryogenic absorption regenerative system after forecooler F1 heat exchange extremely-5 DEG C.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 2MPa, and temperature is-5 DEG C, and desorption process pressure is 0.15MPa, and temperature is 70 DEG C, and the high-concentration waste gas 16 that cryogenic absorption regenerative system is resolved enters into air blast C1 import circular treatment by pipeline.Table 4 is contrasts before and after the process of certain oil plant discharge VOCs waste gas composition.
Certain oil plant of table 4 discharge VOCs waste gas composition and the gas composition after processing
The VOCs exhaust gas concentration of the high concentration processed by compression-direct-cooled-High Pressure Absorption etc. drops to 204ppm, contrast GB (GB16297-1996) related component reaches waste gas emission standard, and the method effectively achieves the process of high concentration, complex component 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 processed
3/ hr), through detecting total concentration up to 26600ppm, VOCs waste gas 1 is entered gas compressor C2 by air blast C1, and the outlet pressure of C2 is 0.5MPa, and temperature 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 forecooler F1, straight touch degree of depth cooling tower T1 pressure is 0.5MPa, straight touch degree of depth cooling tower fluid inlet logistics 9 is the startup cold-producing medium (refrigerating fluid stream) of-20 DEG C, in bottom, the part started in liquid phase organic matter at the bottom of the tower produced after cold-producing medium contacts with VOCs enters waste collection tank V1, and reserved a part of waste liquid enters deep freezer 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, processes by entering High Pressure Absorption system after forecooler F1 heat exchange extremely-2.5 DEG C.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 0.5MPa, and temperature is-2.5 DEG C, and desorption process pressure is 0.12MPa, and temperature is 40 DEG C, and the high-concentration waste gas 16 of cryogenic absorption regenerative system desorb enters into air blast C1 import circular treatment by pipeline.Table 5 is contrasts before and after the process of certain printing enterprise discharge VOCs waste gas composition.
Certain printing enterprise of table 5 discharge VOCs waste gas composition and the gas composition after processing
The VOCs exhaust gas concentration of the high concentration processed by compression-direct-cooled-High Pressure Absorption etc. drops to 305PPM, contrast GB (GB16297-1996) related component reaches waste gas emission standard, and the method effectively achieves the process of high concentration, complex component 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 processed
3/ hr), through detecting total concentration up to 26900ppm, VOCs waste gas 1 is entered gas compressor C2 by air blast C1, and the outlet pressure of C2 is 0.6MPa, and temperature 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 forecooler F1, straight touch degree of depth cooling tower T1 pressure is 0.6MPa, straight touch degree of depth cooling tower fluid inlet logistics 9 adopt-50 DEG C startup cold-producing medium (refrigerating fluid stream), in bottom, the part started in liquid phase organic matter at the bottom of the tower produced after cold-producing medium contacts with VOCs enters waste collection tank V1, and reserved a part of waste liquid enters deep freezer F2 and is cooled to-50 DEG C as above-mentioned startup cold-producing medium.Straight touch degree of depth cooling tower gaseous phase outlet logistics 5 temperature is-45 DEG C, processes by entering cryogenic absorption regenerative system after forecooler F1 heat exchange extremely-5 DEG C.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, and the high-concentration waste gas 16 of cryogenic absorption regenerative system desorb enters into air blast C1 import circular treatment by pipeline.Table 6 is contrasts before and after the process of certain coatings enterprises discharge VOCs waste gas composition.
Certain coatings enterprises of table 6 discharge VOCs waste gas composition and the gas composition after processing
The VOCs exhaust gas concentration of the high concentration processed by compression-direct-cooled-High Pressure Absorption etc. drops to 375PPM, contrast GB (GB16297-1996) related component reaches waste gas emission standard, and the method effectively achieves the process of high concentration, complex component VOCs waste gas.
A kind of process processing VOCs waste gas that the present invention proposes, be described by preferred embodiment, person skilled obviously can not depart from content of the present invention, spirit and scope structure as herein described and technical method are changed or suitably change with 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 all deemed to be included in spirit of the present invention, scope and content.
Claims (8)
1. process a method for 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 lowered the temperature with cryogen heat exchange, is obtained the waste gas after precooling;
B waste gas after the described precooling deriving from step (a) is imported straight touch degree of depth cooling device by (), by lowering the temperature with the refrigerating fluid stream direct contact heat transfer being imported into described straight touch degree of depth cooling device, gas-liquid separation is carried out subsequently in described straight touch degree of depth cooling device, to produce straight touch degree of depth cooling device exit flow and straight touch degree of depth cooling device goes out oral fluid stream, wherein, the part that described straight touch degree of depth cooling device goes out oral fluid stream is collected as waste liquid, another part is after cryogenic system cools further, described straight touch degree of depth cooling device is imported into as described refrigerating fluid stream,
C the described straight touch degree of depth cooling device exit flow deriving from step (b) is heated up as the cryogen described in step (a) by described shell-and-tube heat exchanger and described pending VOC heat exchange by (), deliver to High Pressure Absorption device subsequently to adsorb, obtain the waste gas through High Pressure Absorption process, wherein, after absorption is saturated, desorption and regeneration is carried out to High Pressure Absorption device, and the gas separating sucking-off is passed in the pending described volatile organic compound from waste gas described in step (a);
D () will derive from the described waste gas through High Pressure Absorption process of step (c) after granular active carbon purifying, obtain exhaust up to standard.
2. method according to claim 1, wherein, in step (a), enters gas compressor by described pending waste gas by air blast, imports described shell-and-tube heat exchanger after compression.
3. method according to claim 2, wherein, the outlet pressure of described air blast is 0.1 to 0.15MPa, and the outlet pressure of described gas compressor is 0.5 to 2MPa, and temperature is 30 to 75 DEG C.
4. method according to claim 1, wherein, in step (b), the temperature of the waste gas after described precooling is-20 to 22.5 DEG C, and pressure is 0.5 to 2MPa.
5. method according to claim 1, wherein, in step (c), the temperature of described direct-cooled separator exit flow before entering described shell-and-tube heat exchanger is-80 to-10 DEG C, pressure is 0.5 to 2MPa, and be-25 to 17.5 DEG C by the temperature after described shell-and-tube heat exchanger, pressure is 0.5 to 2MPa.
6. method according to claim 1, wherein, in the High Pressure Absorption device described in step (c), under the pressure of the temperature of-25 to 17.5 DEG C and 0.5 to 2MPa, carries out described High Pressure Absorption process; And by decompression, under the pressure of the temperature of 20 to 70 DEG C and 0.1 to 0.15MPa, carry out described desorption and regeneration.
7. method according to claim 1, wherein, uses at least two High Pressure Absorption devices to realize the continuous process of gas by rotation in step (c).
8., for the treatment of an equipment for volatile organic compound from waste gas, described equipment comprises:
Precooling portion, described precooling portion comprises air blast (C1), gas compressor (C2) and shell-and-tube heat exchanger (F1), wherein, volatile organic compound from waste gas admission line (1) fluid is connected to the entrance of air blast (C1), the outlet fluid of air blast (C1) is connected to the entrance of gas compressor (C2), and the outlet fluid of gas compressor (C2) is connected 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 cooling device (T1), cryogenic system (F2) and waste collecting device (V1), wherein, the tube side outlet fluid of shell-and-tube heat exchanger (F1) is connected to the gas phase entrance of straight touch degree of depth cooling device (T1), straight touch degree of depth cooling device (T1) also has liquid phase entrance, gaseous phase outlet and liquid-phase outlet, described liquid-phase outlet is connected to the material inlet of cryogenic system (F2) by pipeline (7) fluid, the material outlet fluid of cryogenic system (F2) is connected to the liquid phase entrance of straight touch degree of depth cooling device (T1), pipeline (7) has the take-off line (8) be connected with waste collecting device (V1) fluid, the gaseous phase outlet fluid of straight touch degree of depth cooling device (T1) is connected 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 be not less than 2 integer, 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 the outlet of High Pressure Absorption device (P1) to (Pn) is connected with admission line (1) and granular active carbon adsorbent equipment (GAC) difference fluid.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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| JPH04176317A (en) * | 1990-11-08 | 1992-06-24 | Kobe Steel Ltd | Device for concentrating and recovering solvent |
| 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 (4)
| 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 |
| JPH04176317A (en) * | 1990-11-08 | 1992-06-24 | Kobe Steel Ltd | Device for concentrating and recovering solvent |
| 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 |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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| CN104436980B (en) | 2016-09-28 |
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