CN104740889A - Gas treatment method and system - Google Patents
Gas treatment method and system Download PDFInfo
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- CN104740889A CN104740889A CN201410612877.6A CN201410612877A CN104740889A CN 104740889 A CN104740889 A CN 104740889A CN 201410612877 A CN201410612877 A CN 201410612877A CN 104740889 A CN104740889 A CN 104740889A
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Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a gas treatment method and a gas treatment system. The gas treatment method comprises the following steps: feeding the gas to a separation unit for separation; and obtaining a top stream and a bottom stream. A portion of this overhead stream is taken as reflux. The top stream contains the lower boiling material and the bottom stream contains the higher boiling material.
Description
Technical field
The present invention is open about gas processing method and system, the processing method of the gas especially containing organic volatile and system.
Background technology
Many industrial process can produce large quantity of exhaust gas, how effectively to process those waste gas to meet various countries' air pollutant emission specification, and reach energy-conservation, reduce discharging, pollute the object of anti-system, are the targets that industry is constantly made great efforts.Existing many for cleaning high-temp waste gas or the prior art reclaiming organic volatile in waste gas, such as, condensation method, absorption process, absorption method etc.
Condensation method is to reclaim the method for organic volatile in waste gas by direct for high-temperature gas condensation.But the condensation rate of recovery of organic volatile is limited.Moreover, owing to usually having large quantity of moisture in its condensate liquid, make the concentration of organic volatile on the low side, because this increasing the energy consumption of subsequent purification process; Further, the tail gas after its process still containing certain density organic volatile, makes follow-up still need by scrubbing tower to process tail gas usually, and usually need add a large amount of acid/neutralizing treatment liquid during washing, thus quite consumes energy, consumes cost.In addition, condensation method is only applicable to the high boiling point organic compound matter reclaiming high concentration, not good to the recovering effect of low boiling organic volatile.
The application of many use absorption processes is had to be suggested, such as add absorbent/washing agent (such as, water, ethylene glycol phenyl ether, NMP etc.), solidifying agent (such as, water, ethanol, acetone, propyl alcohol etc.) etc. altogether, to reclaim organic volatile in liquid at the bottom of the tower on absorption tower.Also have many technology of absorption process and absorption method that simultaneously utilizes to be reported, after utilizing absorbent to be absorbed by organic volatile, recycling adsorbent (such as, molecular sieve) adsorbs organic volatile.But these methods need extra interpolation absorbent or use adsorbent, and suitable absorbent need be selected for the organic volatile for reclaiming, thus restriction being caused to its application.Moreover, use absorbent or adsorbent to need the reproducer carrying out consuming energy, and can the generations such as a large amount of waste liquids be caused, disadvantageously increase processing cost.Again, absorbent adds the corrosion to equipment, adversely affects absorption efficiency and exhaust-gas treatment ability after absorbing the organic substance in waste gas.In addition, use water as absorbent/washing agent, also make the organic volatile substrate concentration that reclaims in liquid at the bottom of tower on the low side, cause the energy consumption improving subsequent purification process.In addition, also there is the defect of the little and partial adsorbates agent regeneration difficulty of adsorptive selectivity difference, adsorption capacity, and be not suitable for the industrial waste gas of a large amount of discharge of process in the use of adsorbent.Meanwhile, the absorption tower technology of many prior aries, the rate of recovery is on the low side; And it is not it is also only suitable for recovery higher boiling organic volatile, still good to the recovering effect of low boiling organic volatile.In view of this, still need improvement gas processing method and system.
Summary of the invention
The open one of the present invention provides gas processing method, comprising: by this gas containing organic volatile from load point feed-in separator to be separated; And overhead stream is obtained above this load point, below this load point, obtain bottom stream.The backflow of this overhead stream of a part is to contact with this gas in this separator.This overhead stream contains the lower material of boiling point, and bottom this, stream contains the higher material of boiling point.
Moreover the open one of the present invention provides gas handling system, and comprising: separator, comprise packed bed and the load point in order to this gas of feed-in, wherein, this load point is positioned at this separator bottom; And, heat exchanger, for carrying out cooling/condensation to be to obtain overhead stream.This separator of gas feed-in is separated, and to obtain overhead stream above this load point, obtains bottom stream below this load point.The separator of this piece-rate system is designed to make the backflow of this overhead stream of a part to contact with this gas in this separator.
Relative to prior art, by gas processing method of the present invention, the rate of recovery of organic volatile is higher; And organic volatile substrate concentration in product stream is higher, and organic volatile substrate concentration in tail gas is lower, can improve the defect of prior art.Separately, gas processing method of the present invention, does not need additionally to add absorbent/solidifying agent, adsorbent altogether, and the material that separable acquisition gas mid-boiling point is higher and boiling point is lower.
In addition, relative to prior art, by gas handling system of the present invention, the rate of recovery of organic volatile is higher; And organic volatile substrate concentration in product stream is higher, and organic volatile substrate concentration in tail gas is lower, can avoid the defect of prior art.Separately, gas handling system of the present invention, does not need additionally to add absorbent/solidifying agent, adsorbent altogether.And by gas handling system of the present invention, the material that separable acquisition gas mid-boiling point is higher and boiling point is lower.
Accompanying drawing explanation
Figure 1A and Figure 1B is respectively the schematic diagram of the gas processing method according to a specific embodiment;
Fig. 2 A and Fig. 2 B is respectively the schematic diagram of the gas processing method according to a specific embodiment;
Fig. 3 A and Fig. 3 B is respectively the schematic diagram of the gas handling system according to a specific embodiment; And
Fig. 4 A and Fig. 4 B is respectively the schematic diagram of the gas handling system according to a specific embodiment.
Wherein, Reference numeral
1 separator 11 packed bed
12 dispersive element 13 gathering elements
26 outlet 27 entrances
28 load points 29 export
30 outlet 31 outlets
210 entrance 51 heat exchangers
52 heat exchangers
Detailed description of the invention
Below by way of particular specific embodiment, embodiment disclosed by the invention is described, these those skilled in the art can understand other advantages disclosed by the invention and effect by content disclosed in the present specification.The present invention is also implemented by other different specific embodiments or is applied, and the every details in this description also based on different viewpoints and application, can carry out various modification and change under not departing from spirit of the present invention.
Unless otherwise indicated herein, otherwise the singulative " " used in description and claims and " being somebody's turn to do " comprise multiple individuality.
Unless otherwise indicated herein, otherwise the term "or" used in description and claims comprise " and/or " implication.
Gas processing method comprises gas feed-in separator, to obtain overhead stream and bottom stream.Wherein, the backflow of this overhead stream of a part is to contact with the gas in separator, and wherein, this overhead stream contains the lower material of boiling point, and bottom this, stream contains the higher material of boiling point.
Refer to Figure 1A and Figure 1B, it is respectively the schematic diagram of the gas processing method according to a specific embodiment.For the gas of process from load point feed-in (S1) separator to be separated, and above load point, obtain overhead stream (D1), below load point, obtain bottom stream (D2).By this gas processing method, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.In an example, the gas feed-in separator containing organic volatile is separated, to be separated organic volatile.Gas comprises the lower material of boiling point (such as, the organic volatile that boiling point is lower), and the higher material of boiling point (such as, the organic volatile that boiling point is higher), by this gas processing method, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.In an example, the gas feed-in separator containing organic volatile is separated, to obtain concentrated organic volatile.
In an example, the gas feed-in separator containing organic volatile carries out rectifying, to be separated organic volatile.Gas comprises the lower material of boiling point (such as, the organic volatile that boiling point is lower), and the higher material of boiling point (such as, the organic volatile that boiling point is higher), by this gas processing method, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.In an example, the gas feed-in separator containing organic volatile carries out rectifying, to obtain concentrated organic volatile.
As shown in the figure, after gas feed-in separator, ascending vapor becomes overhead stream (D1) after heat exchanger condensation (S5) becomes liquid, wherein, part overhead stream contacts toward load point direction backflow (S2) with the gas in feed-in separator, with the counter current contacting by liquid phase and gas phase, reach the separation of admixture of gas.Descending liquid phase and ascending vapor carry out matter by counter current contacting and pass and pass with heat, the material of boiling point lower (or vapour pressure is higher or more volatile) is moved toward separation unit overhead, and the material of boiling point higher (or vapour pressure is lower or more not volatile) moves toward separation unit bottoms, to reach separation object.Gaseous substance (being sometimes referred to as gas phase composition in literary composition) toward separation unit overhead movement becomes overhead stream (D1) after heat exchanger condensation (S5) becomes liquid, and the liquid phase ingredient toward separation unit bottoms movement then becomes bottom stream (D2) and collects (S7).In an example, the gas feed-in separator containing organic volatile is separated, to be separated organic volatile.Gas comprises the lower material of boiling point (such as, the organic volatile that boiling point is lower), and the higher material of boiling point (such as, the organic volatile that boiling point is higher), by this gas processing method, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.In an example, the gas feed-in separator containing organic volatile carries out rectifying, to be separated organic volatile.Gas comprises the lower material of boiling point (such as, the organic volatile that boiling point is lower), and the higher material of boiling point (such as, the organic volatile that boiling point is higher), by this gas processing method, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.
Part overhead stream is toward load point direction backflow (S2), and another part overhead stream is then discharged (S3) and collects.In overhead stream, for the part and the ratio (such as, S2/S3) of the amount of the non-part for refluxing that reflux, be called reflux ratio.According to a specific embodiment, reflux ratio is 0.1 to 100.
After gas feed-in separator, ascending vapor (gaseous substance toward separation unit overhead movement) becomes overhead stream (D1) after heat exchanger condensation (S5) becomes liquid.According to a specific embodiment, it is become overhead stream after the liquid of 5 DEG C to 50 DEG C that ascending vapor is condensed into temperature by heat exchanger.
The above-mentioned heat exchanger for condensation (but) ascending vapor (gaseous substance toward separation unit overhead movement), can be positioned at separator (as shown in Figure 1A) or be positioned at separator outer (as shown in Figure 1B).For example, the heat exchanger being positioned at separator can be positioned at the top of separator, the ascending vapor in separator (gaseous substance) condensation after heat exchanger (S5) is made to become liquid and become overhead stream (D1), wherein, part overhead stream is toward load point direction backflow (S2), and another part overhead stream is then discharged (S3) separator and collects.Or, heat exchanger can be positioned at outside separator, ascending vapor (gaseous substance) in separator becomes overhead stream (D1) by becoming liquid by condensation (S5) after heat exchanger, wherein, part overhead stream is toward separator (load point direction) backflow (S2), and another part overhead stream is then discharged (S3) and collects.According to a specific embodiment, heat exchanger is condenser.According to a specific embodiment, in heat exchanger, pass into (C1) condensation (but) agent.
In addition, as illustrated in figures ia and ib, after treatment, top gas is had to discharge (S6).After gas feed-in separator is separated, top gas is had to discharge (S6).According to some embodiments, top gas (or the gas that title processed, or claim purified gas, or claim tail gas) be incondensable gas.In certain embodiments, top gas is discharged from the top of this separator.In certain embodiments, top gas automatic heat-exchanger is discharged.The top gas of this discharge can optionally process further again.According to a specific embodiment, the top gas of discharge directly can be disposed to air.According to a specific embodiment, the top gas of discharge can again with wash mill process.
By above-mentioned processing method, the high boiling substance (organic volatile that such as, boiling point is higher) in separable (or concentrated or purification) gas and low-boiling point material (organic volatile that such as, boiling point is lower).According to a specific embodiment, the gas feed-in separator containing organic volatile is separated, and to obtain the lower material of boiling point in overhead stream, in the stream of bottom, obtains the higher material of boiling point.In an example, the gas feed-in separator containing organic volatile is separated, to be separated the lower organic volatile of boiling point and the higher organic volatile of boiling point.In an example, the gas feed-in separator containing organic volatile is separated, to obtain concentrated organic volatile.
According to a specific embodiment, the gas feed-in separator containing organic volatile carries out rectifying, to obtain the lower material of boiling point in overhead stream, in the stream of bottom, obtains the higher material of boiling point.In an example, the gas feed-in separator containing organic volatile carries out rectifying, to be separated the lower organic volatile of boiling point and the higher organic volatile of boiling point.In an example, the gas feed-in separator containing organic volatile carries out rectifying, to obtain concentrated organic volatile.
For the organic volatile in the gas of process, there is no particular restriction.Usually, for the material containing tool different boiling (or vapour pressure or volatility) in the gas of process.For example, the organic volatile of tool different boiling (or vapour pressure or volatility) can be contained in the gas for process.The example of organic volatile includes, but not limited to dimethylacetylamide (N, N-Dimethylacetamide, DMAc), acetic acid (Acetic acid, HAc), METHYLPYRROLIDONE (N-Methyl-2-pyrrolidone, NMP), dimethyl formamide (N, N-Dimethylformamide, DMF), pyridine (Pyridine), picoline (Methyl-Pyridine) (as, 3-picoline (3-Methyl-Pyridine (3-MP)), α-Picoline (α-methylpyridine), β-Picoline (beta-picoline), γ-Picoline (γ-picoline)), propylene glycol monomethyl ether (PGME) is (as 1-methoxy-2-propanol (1-Methoxy-2-propanol), 2-methoxy-1-propanol (2-Methoxy-1-propanol)), propylene glycol monomethyl ether acetate (Propylene Glycol Mono-methylEther Acetate, PGMEA), dimethyl sulfoxide (DMSO) (Dimethyl sulfoxide, DMSO), ethyl acetate (Ethyl Acetate, EAC), ethylene glycol (Ethylene Glycol, EG), diethylene glycol (DiethyleneGlycol, DEG), triethylene glycol (Triethylene Glycol, TEG), propane diols (Propylene Glycol, PG), BDO (Isosorbide-5-Nitrae-butanediol), diethylene glycol monobutyl ether (diethylene glycol monobutylether, BDG), MEA (Monoethanolamine, MEA), ethylenediamine (Ethylenediamine), acrylic acid (Acrylic acid), methacrylic acid (2-methylpropenoic acid), glycol monoethyl ether (2-Methoyxethanol), ethylene glycol monoethyl ether (2-Ethoxyethanol), dioxane (Dioxane), butanols (butyl alcohol), 2-butanols (2-butyl alcohol), isobutanol (Isobutyl alcohol), 1, 4-butanediol (1, 4-butanediol), terpineol (Terpineol), alcohol ester 12 (Texanol) and combination thereof.According to some embodiments, for containing dimethylacetylamide (DMAc), acetic acid, METHYLPYRROLIDONE (NMP), dimethyl formamide (DMF), 3-picoline and/or its combination in the gas of process.
According to a specific embodiment, the direct feed-in separator of the high-temperature gas containing organic volatile is separated.Temperature for the gas of process can be, such as, and 50 DEG C to 250 DEG C.In an example, be that the gas feed-in separator containing organic volatile of 50 DEG C to 250 DEG C is to be separated by temperature.In an example, be that the gas feed-in separator containing organic volatile of 70 DEG C to 80 DEG C is to be separated by temperature.According to a specific embodiment, the direct feed-in separator of the high-temperature gas containing organic volatile carries out rectifying.In an example, be that the gas feed-in separator containing organic volatile of 50 DEG C to 250 DEG C is to carry out rectifying by temperature.In an example, be that the gas feed-in separator containing organic volatile of 70 DEG C to 80 DEG C is to carry out rectifying by temperature.
Gas processing method/system disclosed by the invention and prior art use condensation method or absorption/absorption method process gas, and person is different.In addition, method/system disclosed by the invention also uses destilling tower person different from prior art.Prior art uses the material of its feed-in of destilling tower person to be liquid, and it need arrange reboiler (needing by extraneous supplied heat source) at the bottom of tower, uses the material (medium of heating is generally steam or deep fat) of heating feedback material.And the material handled by gas processing method/system disclosed by the invention is the gas (high-temperature gas such as containing organic volatile) containing organic volatile, therefore, the feedback material of feed-in gas handling system is for the gas containing organic volatile and on-liquid, so do not need to supply thermal source by the external world, and without the need to arranging reboiler.
According to a specific embodiment, the direct feed-in separator of the high-temperature gas containing organic volatile is separated, and to obtain the overhead stream containing the lower material of boiling point above load point, and below load point, obtains the bottom stream containing the higher material of boiling point.In an example, the direct feed-in separator of high-temperature gas containing organic volatile is separated, to obtain the overhead stream containing the lower organic volatile of boiling point above load point, and below load point, obtain the bottom stream containing the higher organic volatile of boiling point.In an example, the direct feed-in separator of the high-temperature gas containing organic volatile is separated, to obtain the bottom stream containing the higher organic volatile of boiling point below load point.
According to a specific embodiment, the direct feed-in separator of the high-temperature gas containing organic volatile carries out rectifying, to obtain the overhead stream containing the lower material of boiling point above load point, and below load point, obtains the bottom stream containing the higher material of boiling point.In an example, the direct feed-in separator of high-temperature gas containing organic volatile carries out rectifying, to obtain the overhead stream containing the lower organic volatile of boiling point above load point, and below load point, obtain the bottom stream containing the higher organic volatile of boiling point.In an example, the direct feed-in separator of the high-temperature gas containing organic volatile carries out rectifying, to obtain the bottom stream containing the higher organic volatile of boiling point below load point.
According to some embodiments, the direct feed-in separator of the high-temperature gas containing organic volatile is separated, to obtain the bottom stream containing the higher organic volatile of boiling point below load point.According to some embodiments, the direct feed-in separator of the high-temperature gas containing organic volatile carries out rectifying, to obtain the bottom stream containing the higher organic volatile of boiling point below load point.The example of the organic volatile that boiling point is higher includes, but not limited to dimethylacetylamide (N, N-Dimethylacetamide, DMAc), acetic acid (Aceticacid, HAc), METHYLPYRROLIDONE (N-Methyl-2-pyrrolidone, NMP), dimethyl formamide (N, N-Dimethylformamide, DMF), pyridine (Pyridine), picoline (Methyl-Pyridine) (as, 3-picoline (3-Methyl-Pyridine (3-MP)), α-Picoline (α-methylpyridine), β-Picoline (beta-picoline), γ-Picoline (γ-picoline)), propylene glycol monomethyl ether (PGME) is (as 1-methoxy-2-propanol (1-Methoxy-2-propanol), 2-methoxy-1-propanol (2-Methoxy-1-propanol)), propylene glycol monomethyl ether acetate (Propylene Glycol Mono-methylEther Acetate, PGMEA), dimethyl sulfoxide (DMSO) (Dimethyl sulfoxide, DMSO), acetic acid esters (EthylAcetate, EAC), ethylene glycol (Ethylene Glycol, EG), diethylene glycol (Diethylene Glycol, DEG), triethylene glycol (Triethylene Glycol, TEG), propane diols (Propylene Glycol, PG), BDO (Isosorbide-5-Nitrae-butanediol), diethylene glycol monobutyl ether (diethylene glycol monobutylether, BDG), MEA (Monoethanolamine, MEA), ethylenediamine (Ethylenediamine), acrylic acid (Acrylic acid), 2-methacrylic acid (2-methylpropenoic acid), glycol monoethyl ether (2-Methoyxethanol), ethylene glycol monoethyl ether (2-Ethoxyethanol), dioxane (Dioxane), butanols (butyl alcohol), 2-butanols (2-butyl alcohol), isobutanol (Isobutyl alcohol), 1, 4-butanediol (1, 4-butanediol), terpineol (Terpineol), alcohol ester 12 (Texanol) and combination thereof.In certain embodiments, the organic volatile that boiling point is higher is dimethylacetylamide (DMAc), acetic acid, METHYLPYRROLIDONE (NMP), dimethyl formamide (DMF) and/or its combination.
Herein, material/organic volatile that boiling point is higher, refers to for material/organic volatile lower relative to the composition mid-boiling point of admixture of gas, boiling point the higher person.For example, after being processed by admixture of gas feed-in separator, relative the higher person of composition mid-boiling point of admixture of gas can obtain from bottom stream, and the relatively low person of composition mid-boiling point of admixture of gas can obtain from overhead stream.
In addition, according to some embodiments, part bottom stream moves to above load point.According to some embodiments, part bottom is flowed back to and is flow to above load point.In certain embodiments, part bottom stream returns separator.In certain embodiments, after part bottom flows through heat exchange, return separator (backflow).See Fig. 2 A and Fig. 2 B, it is respectively the schematic diagram of the gas processing method according to a specific embodiment.As shown in the figure, after obtaining (D2) bottom stream, part bottom stream (S4) carries out refluxing (returning separator) after heat exchange (S8) through heat exchanger, flows, discharge and collect (S7) bottom remaining.Part bottom stream is circulated to and (returns separator) above load point (S4), the chance of liquid gas contact in separator can be increased, improve the usefulness (separating effect) of separator/gas treatment.According to a specific embodiment, heat exchanger is condenser.Optionally can adjust the amount of the bottom stream returning separator.
Above-mentioned heat exchanger makes to carry out lower the temperature/cool (S8) for the part returning separator in the stream of bottom.In some embodiments, the cooling agent that heat exchange uses is from overhead stream.In some embodiments, the cooling agent in heat exchanger is from the part for refluxing non-in overhead stream.For example, non-part (S3) for refluxing in overhead stream (desirable its part or all of) can be utilized, as the cooling agent in heat exchanger, in flowing with bottom, carry out heat exchange for the part of reflux (returning separator).In certain embodiments, in overhead stream, non-(or being discharge separator in certain embodiments) for refluxing partly (S3), the desirable cooling agent that it is partly or entirely used as in heat exchanger, flows through to make part bottom after this heat exchanger carries out lowering the temperature/cool and refluxes (returning separator).
Above-mentioned gas processing method, by being separated by the separator of gas feed-in gas handling system, to implement the separation (or concentrated or purification) of organic volatile.According to a specific embodiment, above-mentioned gas processing method, by the separator of gas feed-in gas handling system is carried out gas-liquid separation, to implement the separation (or concentrated or purification) of organic volatile.According to a specific embodiment, above-mentioned gas processing method, by the separator of gas feed-in gas handling system is carried out rectifying, to implement the separation (or concentrated or purification) of organic volatile
Gas handling system comprises separator and heat exchanger.
In some embodiments, separator has rectification cell.According to a specific embodiment, separator is rectifier unit (such as, rectifying column).
Separator, comprises packed bed and the load point in order to feed-in gas.According to a specific embodiment, load point is positioned at the bottom of separator.In an example, high-temperature gas is directly by being positioned at the load point feed-in separator of separator bottom to be separated.In an example, high-temperature gas is directly by being positioned at the load point feed-in separator of separator bottom to carry out rectifying.
Refer to Fig. 3 A and Fig. 3 B, it is respectively the schematic diagram of the gas handling system according to a specific embodiment.
Gas handling system comprises separator 1 and heat exchanger 51.
Separator 1, comprises packed bed 11 and load point 28.The quantity of packed bed 11 can optionally be selected.In an example, separator 1 comprises one or more packed bed 11.
According to a specific embodiment, the material of packed bed 11 containing bigger serface (surface areas per unit volumes), its role is to the area increasing gas-liquid contact.Packed bed makes the liquid of overhead reflux by forming a high surface area film after packed bed and contacting with each other with the gas phase risen, and then reaches the object of gas-liquid separation.According to a specific embodiment, above packed bed 11, be provided with dispersive element 12.According to a specific embodiment, the effect of dispersive element 12 is that the descending liquid of order backflow is evenly distributed.According to a specific embodiment, below packed bed 11, be provided with gathering element 13.According to a specific embodiment, the effect of gathering element 13 is collect descending liquid and mix.
Optionally can adjust the height of packed bed 11.For example, the height of packed bed 11 can be arranged according to actual needs, such as, can be 0.3 meter high to 10 meters.The structure of packed bed 11 can be has dumped packing, and filler can be arbitrary shape.For example, the filler being of a size of 1/8 inch to 3 inch can be used.Or the structure of packed bed 11 can be has structured packing, and filler is regularly arranged according to the size of packed bed.The packing material (being sometimes referred to as filler) of packed bed 11 can be, such as, but not limited to: metal species, Plastic, ceramic-like or its combination.
Load point 28 is positioned at the bottom of separator 1.In an example, load point 28 is positioned at the below of packed bed 11.Gas processes from load point 28 feed-in separator 1, and wherein, ascending vapor becomes overhead stream after being condensed into liquid by heat exchanger 51.According to a specific embodiment, condensation temperature is 5 DEG C to 50 DEG C.
Separator 1 is designed to make overhead stream backflow (being generally liquid phase) of a part to contact with the gas in separator 1.By the counter current contacting of liquid phase and gas phase, the separation of gas mixture can be reached.By the counter current contacting of descending liquid phase and ascending vapor, the material of boiling point lower (or vapour pressure is higher or more volatile) can be made to move toward the top of separator 1, and the material of boiling point higher (or vapour pressure is lower or more not volatile) moves toward the bottom of separator 1, to reach the object of separation.Gaseous substance (gas phase composition) toward the top movement of separator 1 becomes overhead stream after being condensed into liquid by heat exchanger 51, and wherein, a part of overhead stream is toward the backflow of load point 28 direction, and another part overhead stream is then discharged and collects.In an example, a part of overhead stream discharges separator 1 by outlet 30.Moreover the liquid phase substance (liquid phase ingredient) toward the bottom movement of separator 1 then becomes bottom stream and collects.In an example, bottom flows through outlet 29 and discharges separator 1.
According to a specific embodiment, the separator 1 of the gas feed-in gas handling system containing organic volatile is separated, to be separated organic volatile.Gas comprises the lower material of boiling point (such as, the organic volatile that boiling point is lower), and the higher material of boiling point (such as, the organic volatile that boiling point is higher), by this gas handling system, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.In an example, the separator 1 of the gas feed-in gas handling system containing organic volatile is separated, to obtain concentrated organic volatile in the stream of bottom.
According to a specific embodiment, the separator 1 of the gas feed-in gas handling system containing organic volatile carries out rectifying, to be separated organic volatile.Gas comprises the lower material of boiling point (such as, the organic volatile that boiling point is lower), and the higher material of boiling point (such as, the organic volatile that boiling point is higher), by this gas handling system, the material (for the material higher relative to gas mid-boiling point) that gas mid-boiling point is lower obtains in overhead stream, and the material that gas mid-boiling point is higher then obtains in bottom stream.In an example, the separator 1 of the gas feed-in gas handling system containing organic volatile carries out rectifying, to obtain concentrated organic volatile in the stream of bottom.
In overhead stream, for the part and the ratio (such as, S2/S3) of the amount of the non-part for refluxing that reflux, be called reflux ratio.According to a specific embodiment, the separator of gas handling system is designed to make reflux ratio be 0.1 to 100 (by weight).
For the heat exchanger 51 of condensation (but) ascending vapor (gaseous substance toward the top movement of separator 1), separator 1 (as shown in Figure 3A) can be positioned at or be positioned at separator 1 outer (as shown in Figure 3 B).For example, as shown in Figure 3A, the heat exchanger 51 being positioned at separator 1 can be positioned at the top of separator 1, the ascending vapor in separator (gaseous substance) is made to become overhead stream by being condensed into liquid after heat exchanger 51, wherein, part overhead stream is toward the backflow of load point 28 direction, and another part overhead stream is then discharged separator 1 and collects.Or, as shown in Figure 3 B, heat exchanger 51 can be positioned at outside separator 1, ascending vapor (gaseous substance) in separator is by outlet 31 to heat exchanger 51, overhead stream is become after being condensed into liquid by heat exchanger 51, wherein, a part of overhead stream is back in separator 1 by entrance 27, and another part overhead stream is then discharged and collects.According to a specific embodiment, heat exchanger 51 is condenser.Condensation (but) agent in heat exchanger 51 can be, such as, and water.
In addition, as shown in Fig. 3 A and Fig. 3 B, after treatment, top gas is had to discharge from outlet 26.After gas feed-in separator carries out gas-liquid separation, top gas is had to discharge from outlet 26.According to some embodiments, top gas (or the gas that title processed, or claim purified gas, or claim tail gas), be incondensable gas.In certain embodiments, top gas is discharged from the top of this separator 1.In certain embodiments, top gas automatic heat-exchanger 51 is discharged.According to a specific embodiment, gas handling system also comprises the device for processing top gas further.In an example, the top gas of discharge directly can be disposed to air.In an example, gas handling system also comprises the wash mill for the treatment of the top gas of discharging from outlet 26.
By above-mentioned gas treatment system, the high boiling substance (organic volatile that such as, boiling point is higher) in separable (or concentrated or purification) gas and low-boiling point material (organic volatile that such as, boiling point is lower).According to a specific embodiment, the gas feed-in gas handling system containing organic volatile is separated, and to obtain the lower material of boiling point in overhead stream, in the stream of bottom, obtains the higher material of boiling point.In an example, the gas feed-in gas handling system containing organic volatile is separated, to be separated the lower organic volatile of boiling point and the higher organic volatile of boiling point.In an example, the gas feed-in gas handling system containing organic volatile is separated, to obtain concentrated organic volatile.In an example, the gas feed-in gas handling system containing organic volatile is separated, to obtain concentrated organic volatile in the stream of bottom.
According to a specific embodiment, the gas feed-in gas handling system containing organic volatile carries out rectifying, to obtain the lower material of boiling point in overhead stream, in the stream of bottom, obtains the higher material of boiling point.In an example, the gas feed-in gas handling system containing organic volatile carries out rectifying, to be separated the lower organic volatile of boiling point and the higher organic volatile of boiling point.In an example, the gas feed-in gas handling system containing organic volatile carries out rectifying, to obtain concentrated organic volatile.In an example, the gas feed-in gas handling system containing organic volatile carries out rectifying, to obtain concentrated organic volatile in the stream of bottom.
According to a specific embodiment, the high-temperature gas containing organic volatile is directly separated from load point 28 feed-in separator 1.Temperature for process gas can be, such as, and 50 DEG C to 250 DEG C.In an example, be that the gas containing organic volatile of 50 DEG C to 250 DEG C is from load point 28 feed-in separator 1 by temperature.In an example, be that the gas containing organic volatile of 70 DEG C to 80 DEG C is from load point 28 feed-in separator 1 by temperature.
According to a specific embodiment, high-temperature gas containing organic volatile directly carries out rectifying from load point 28 feed-in separator 1, to obtain the overhead stream containing the lower material of boiling point above load point 28, and below load point 28, obtain the bottom stream containing the higher material of boiling point.In an example, high-temperature gas containing organic volatile directly carries out rectifying from load point 28 feed-in separator 1, to obtain the overhead stream containing the lower organic volatile of boiling point above load point 28, and below load point 28, obtain the bottom stream containing the higher organic volatile of boiling point.In an example, the high-temperature gas containing organic volatile directly carries out rectifying from load point 28 feed-in separator 1, to obtain the bottom stream containing the higher organic volatile of boiling point below load point 28.In an example, the high-temperature gas containing organic volatile directly carries out rectifying from load point 28 feed-in separator 1, to obtain the bottom stream containing concentrated organic volatile below load point 28.
In addition, according to some embodiments, bottom stream is discharged separator 1 and collects.According to some embodiments, separator is designed to part bottom stream is moved to above load point 28.According to some embodiments, separator is designed to make part bottom flow back to stream.In certain embodiments, the separator 1 of piece-rate system is designed to part bottom is flowed back to (returning separator 1).In certain embodiments, backflow (returning separator 1) after part bottom flows through heat exchange.See Fig. 4 A and Fig. 4 B, it is respectively the schematic diagram of the gas handling system according to a specific embodiment.As shown in the figure, gas handling system also comprises another heat exchanger 52, and part bottom flows through after heat exchanger 52 carries out heat exchange is refluxed (returning separator 1) by entrance 210, flows, discharge and collect bottom remaining.(being circulated to above load point 28) (returning separator 1) is flowed back in order part bottom, the chance of the liquid gas contact in separator 1 can be increased, improve the usefulness (separating effect) of separator 1 (gas handling system).According to a specific embodiment, heat exchanger 52 is cooler/condenser.
Above-mentioned heat exchanger 52 makes to cool for the part returning separator 1 in the stream of bottom.In some embodiments, the cooling agent in heat exchanger 52 is from overhead stream; Specifically, the cooling agent in heat exchanger 52 is from the part for refluxing non-in overhead stream.For example, non-part for refluxing in overhead stream (desirable its part or all of) can being utilized, as the cooling agent in heat exchanger 52, in flowing with bottom, carrying out heat exchange for the part returning separator 1.In certain embodiments, non-(or being discharge separator 1 in certain embodiments) part for refluxing in overhead stream, it is desirable that it is part or all of, as the cooling agent in heat exchanger 52, cool/lower the temperature reflux (returning separator 1) after flowing through this heat exchanger 52 to make part bottom.
Above-mentioned gas processing method, can be used for process, such as high-temperature gas (high-temperature gas such as, containing organic volatile).For example, above-mentioned gas processing method, can be used for process high-temp waste gas (high-temp waste gas such as, containing organic volatile).By above-mentioned gas processing method, the organic volatile (high and low boilers) in separable/concentrated/purification/removal/gas recovery (such as, high-temp waste gas).
By above-mentioned gas treatment system, can process, such as high-temperature gas (high-temperature gas such as, containing organic volatile).For example, by above-mentioned gas treatment system, high-temp waste gas (high-temp waste gas such as, containing organic volatile) can be processed.By above-mentioned gas treatment system, the organic volatile (high and low boilers) in separable/concentrated/purification/removal/gas recovery (such as, high-temp waste gas).
The present invention will be further illustrated by embodiment, but the category of these embodiments not for limiting this exposure.Unless specifically stated otherwise, in the following example and comparing embodiment for represent any composition content and, if having, " % " and " part " of any amount of substance take weight as benchmark.
Embodiment:
Embodiment 1
Gas treatment is carried out with the gas processing method/system corresponding to Fig. 2 B/4B schematic diagram.By high-temperature gas feed-in (S1) separator, hot-gas temperature is 80 DEG C, air quantity is 100NCMM (standard cube m/min), and high-temperature gas contains air 97.4 % by weight (wt%), water 1.4wt%, dimethylacetylamide (DMAC) 1.1wt%, acetic acid 0.1wt%.Pass into the cooling/solidifying agent of (S5) low-temperature cooling water (C1) as cooler/condenser in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 10 DEG C and flows down.Overhead stream backflow (S2) of a part returns separator to contact with the gas in feed-in separator, and remaining overhead stream (the non-part for refluxing) (S3) then flow to another heat exchanger (52) as (S8) cooling agent.In adjustment condensate liquid (overhead stream), the ratio of S2/S3 is 3.8.Obtain (D2) bottom stream in separation unit bottoms outlet, shunting bottom stream is for S4 and S7, S4 flow-control is at 30 kgs/hr (kg/hr), and S4 returns separator.After system stability, obtain (S7) concentrate in outlet, concentrate is containing dimethylacetylamide (DMAc) 85.3wt%, acetic acid (HAc) 9.5wt% and water 5.2wt%.Gas after outlet (26) obtains (S6) purification, after purification, gas is containing dimethylacetylamide 0.05ppm and acetic acid 1.1ppm.(ppm calculates with mg/kg).The rate of recovery 99% of organic volatile dimethylacetylamide, the rate of recovery 99% of acetic acid.The computational methods of the rate of recovery to flow back to the ratio of the weight of the organic volatile in the weight of receipts (S7) and feed-in (S1) separator in this gas in bottom for this organic volatile.Namely in S7 the weight of this organic substance divided by the weight of this organic substance in S1.
Comparative example 1-prior art condensation method
By 80 DEG C of high-temperature gases described in embodiment 1 directly with the condensation method process of prior art.This strand of high-temperature gas is condensed to 10 DEG C, and condensed condensate liquid is containing dimethylacetylamide (DMAc) 54.3wt%, acetic acid (HAc) 6.3wt% and water 39.4wt%.The emission gases (after purification gas) be not condensed is containing dimethylacetylamide 625ppm and acetic acid 14ppm.The rate of recovery 94.4% of the organic volatile dimethylacetylamide adopting condensation method to obtain, the rate of recovery 98.8% of acetic acid.The computational methods of the condensation method rate of recovery are the ratio of the weight of this organic volatile in the weight of this organic volatile in condensate liquid and feed-in condenser.
Embodiment 2
Gas treatment is carried out with the gas processing method/system corresponding to Fig. 2 B/4B schematic diagram.By high-temperature gas feed-in (S1) separator, hot-gas temperature is 80 DEG C, air quantity is 100NCMM (standard cube m/min), and high-temperature gas contains air 97.4 % by weight (wt%), water 1.4wt%, dimethylacetylamide (DMAC) 1.1wt%, acetic acid 0.1wt%.Pass into the cooling/solidifying agent of (S5) low-temperature cooling water (C1) as cooler/condenser in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 10 DEG C and flows down.Overhead stream backflow (S2) of a part returns separator to contact with the gas in feed-in separator, and remaining overhead stream (the non-part for refluxing) (S3) then flow to another heat exchanger (52) as (S8) cooling agent.In adjustment condensate liquid (overhead stream), the ratio of S2/S3 is 3.0.Obtain (D2) bottom stream in separation unit bottoms outlet, shunting bottom stream is for S4 and S7, S4 flow-control is at 30 kgs/hr (kg/hr), and S4 returns separator.Until system reach stable after, obtain (S7) concentrate in outlet, concentrate is containing dimethylacetylamide (DMAc) 88.2wt%, acetic acid (HAc) 10.9wt% and water 0.9wt%.Gas after outlet (26) obtains (S6) purification, after purification, gas is containing dimethylacetylamide 0.05ppm and acetic acid 1.1ppm.(ppm calculates with mg/kg).The rate of recovery 99% of organic volatile dimethylacetylamide, the rate of recovery 99% of acetic acid.The computational methods of the rate of recovery to flow back to the ratio of the weight of the organic volatile in the weight of receipts (S7) and feed-in (S1) separator in this gas in bottom for this organic volatile.Namely in S7 the weight of this organic substance divided by the weight of this organic substance in S1.
Embodiment 3
Gas treatment is carried out with the gas processing method/system corresponding to Fig. 2 B/4B schematic diagram.By high-temperature gas feed-in (S1) separator, hot-gas temperature is 70 DEG C, air quantity is 100NCMM (standard cube m/min), and high-temperature gas contains air 97.4 % by weight (wt%), water 1.4wt%, dimethylacetylamide (DMAC) 1.1wt%, acetic acid 0.1wt%.Pass into the cooling/solidifying agent of (S5) low-temperature cooling water (C1) as cooler/condenser in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 10 DEG C and flows down.Overhead stream backflow (S2) of a part returns separator to contact with the gas in feed-in separator, and remaining overhead stream (the non-part for refluxing) (S3) then flow to another heat exchanger (52) as (S8) cooling agent.In adjustment condensate liquid (overhead stream), the ratio of S2/S3 is 3.8.Obtain (D2) bottom stream in separation unit bottoms outlet, shunting bottom stream is for S4 and S7, S4 flow-control is at 30 kgs/hr (kg/hr), and S4 returns separator.Until system reach stable after, obtain (S7) concentrate in outlet, concentrate is containing dimethylacetylamide (DMAc) 80.8wt%, acetic acid (HAc) 9.0wt% and water 10.2wt%.Gas after outlet (26) obtains (S6) purification, after purification, gas is containing dimethylacetylamide 0.06ppm and acetic acid 1.2ppm.(ppm calculates with mg/kg).The rate of recovery 99% of organic volatile dimethylacetylamide, the rate of recovery 99% of acetic acid.The computational methods of the rate of recovery to flow back to the ratio of the weight of the organic volatile in the weight of receipts (S7) and feed-in (S1) separator in this gas in bottom for this organic volatile.Namely in S7 the weight of this organic substance divided by the weight of this organic substance in S1.
Embodiment 4
Gas treatment is carried out with the gas processing method/system of the schematic diagram corresponding to Fig. 2 B/4B.By high-temperature gas feed-in (S1) separator, hot-gas temperature is 70 DEG C, air quantity is 100NCMM (standard cube m/min), and high-temperature gas contains air 97.4 % by weight (wt%), water 1.4wt%, dimethylacetylamide (DMAC) 1.1wt%, acetic acid 0.1wt%.Pass into the cooling/solidifying agent of (S5) low-temperature cooling water (C1) as cooler/condenser in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 12 DEG C and flows down.Overhead stream backflow (S2) of a part returns separator to contact with the gas in feed-in separator, and remaining overhead stream (the non-part for refluxing) (S3) then flow to another heat exchanger (52) as (S8) cooling agent.In adjustment condensate liquid (overhead stream), the ratio of S2/S3 is 3.8.Obtain (D2) bottom stream in separation unit bottoms outlet, shunting bottom stream is for S4 and S7, S4 flow-control is at 30 kgs/hr (kg/hr), and S4 returns separator.Until system reach stable after, obtain (S7) concentrate in outlet, concentrate is containing dimethylacetylamide (DMAc) 86.9wt%, acetic acid (HAc) 9.6wt% and water 3.5wt%.Gas after outlet (26) obtains (S6) purification, after purification, gas is containing dimethylacetylamide 0.1ppm and acetic acid 1.6ppm.(ppm calculates with mg/kg).The rate of recovery 99.9% of organic volatile dimethylacetylamide, the rate of recovery 99.9% of acetic acid.The computational methods of the rate of recovery to flow back to the ratio of the weight of the organic volatile in the weight of receipts (S7) and feed-in (S1) separator in this gas in bottom for this organic volatile.Namely in S7 the weight of this organic substance divided by the weight of this organic substance in S1.
Embodiment 5
Gas treatment is carried out with the gas processing method/system corresponding to Figure 1B/3B schematic diagram.By high-temperature gas feed-in (S1) separator, hot-gas temperature is 70 DEG C, air quantity is 100NCMM (standard cube m/min), and high-temperature gas contains air 97.4 % by weight (wt%), water 1.4wt%, dimethylacetylamide (DMAC) 1.1wt%, acetic acid 0.1wt%.Pass into the cooling/solidifying agent of (S5) low-temperature cooling water (C1) as cooler/condenser in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 12 DEG C and flows down.Overhead stream backflow (S2) of a part returns separator to contact with the gas in feed-in separator.In adjustment condensate liquid (overhead stream), the ratio of S2/S3 is 3.8.(D2) bottom stream is obtained in separation unit bottoms outlet.Until system reach stable after, obtain (S7) concentrate in outlet, concentrate is containing dimethylacetylamide (DMAc) 86.4wt%, acetic acid (HAc) 9.6wt% and water 4wt%.Gas after outlet (26) obtains (S6) purification, after purification, gas is containing dimethylacetylamide 0.02ppm and acetic acid 0.01ppm.(ppm calculates with mg/kg).The rate of recovery 99.6% of organic volatile dimethylacetylamide, the rate of recovery 99.9% of acetic acid.The computational methods of the rate of recovery to flow back to the ratio of the weight of the organic volatile in the weight of receipts (S7) and feed-in (S1) separator in this gas in bottom for this organic volatile.Namely in S7 the weight of this organic substance divided by the weight of this organic substance in S1.
Above-described embodiment 1 to 5 and comparative example 1 as shown in table 1 below.
Table 1
Note: the label (S1, S2, S3, S4, S6, S7, D1 etc.) in form is applicable to embodiment and reference Fig. 2 B/4B or Figure 1B/3B.
Embodiment 6
Gas treatment is carried out with the gas processing method/system corresponding to Figure 1B/3B schematic diagram, by high-temperature gas feed-in (S1) separator, hot-gas temperature is 80 DEG C, air quantity is 100NCMM (standard cube m/min), high-temperature gas contains air 98.6wt%, water 1.1wt%, METHYLPYRROLIDONE (NMP) 0.3wt%, cooling/solidifying the agent of (S5) low-temperature cooling water (C1) as cooler/condenser is passed in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 10 DEG C and flows down, the ratio of adjustment condensate liquid S2/S3 is 6.4, S2 returns separator, S3 then discharges collection.Until system reach stable after, obtain (S7) concentrate METHYLPYRROLIDONE (NMP) 99.3wt%, water 0.7wt% in outlet.After purification, gas S6 obtains METHYLPYRROLIDONE (NMP) 1ppm in outlet.
Comparative example 2-prior art condensation method
By high-temperature gas feed-in one condenser described in embodiment 6, a part is directly condensed into the liquid of 10 DEG C, becomes liquid at the bottom of tower, concentrate METHYLPYRROLIDONE (NMP) 39.5wt%, water 60.5wt%.The organic volatile rate of recovery 97.3%, comparatively embodiment 6 is low.And in concentrate, the concentration of organic volatile is on the low side, because this increasing the energy cost of subsequent purification process organic volatile.Another part is uncondensed gas is then exhaust (tail gas), and in exhaust, the concentration 69ppm of organic volatile, still need process with scrubbing tower, and need add a large amount of acid/neutralizing treatment liquid and thus consume energy, consume cost during washing.
Comparative example 3-prior art absorption process
By the high-temperature gas described in embodiment 6 by bottom feed-in one absorption tower, and add absorbent (as: water) 159kg/hr in top, liquid at the bottom of tower, concentrate METHYLPYRROLIDONE (NMP) 60.9wt%, water 39.1wt%.In concentrate, the concentration of organic volatile is on the low side, because this increasing the energy cost of subsequent purification process organic volatile.Another part is uncondensed gas is then exhaust (tail gas), and in exhaust, the concentration 30ppm of organic volatile, still need process with scrubbing tower, and need add a large amount of acid/neutralizing treatment liquid and thus consume energy, consume cost during washing.
Above-described embodiment 6 and comparative example 2 and 3 as shown in table 2 below.
Embodiment 7
Gas treatment is carried out with the gas processing method/system corresponding to Fig. 2 B/4B schematic diagram.By high-temperature gas feed-in (S1) separator, hot-gas temperature is 80 DEG C, air quantity is 100NCMM (standard cube m/min), and high-temperature gas contains air 97.4wt%, water 1.39wt%, dimethylacetylamide (DMAC) 1.15wt%, 3-picoline (3-MP) 0.06wt%.Pass into the cooling/solidifying agent of (S5) low-temperature cooling water (C1) as cooler/condenser in heat exchanger (cooler/condenser), and the gas through heat exchanger risen after making feed-in separator is condensed into liquid (overhead stream) (D1) of 10 DEG C and flows down.Overhead stream backflow (S2) of a part returns separator to contact with the gas in feed-in separator, and remaining overhead stream (the non-part for refluxing) (S3) then flow to another heat exchanger (52) as (S8) cooling agent.In adjustment condensate liquid (overhead stream), the ratio of S2/S3 is 4.Obtain (D2) bottom stream in separation unit bottoms outlet, shunting bottom stream is for S4 and S7, S4 flow-control is at 30 kgs/hr (kg/hr), and S4 returns separator.Until system reach stable after, obtain (S7) concentrate in outlet at bottom, concentrate dimethylacetylamide 89.6%, 3-picoline 1.7wt%, water 8.7wt%.And separately obtain overhead stream recovery (S3) concentrate 3-picoline 3.4wt%, water 96.6wt% in outlet.After purification, gas (S6) obtains dimethylacetylamide 1ppm, 3-picoline 209ppm in outlet (26).(ppm calculates with mg/kg).The rate of recovery 31.4% of the rate of recovery 99.9%, the 3-picoline of organic volatile dimethylacetylamide.The computational methods of dimethylacetylamide (DMAc) rate of recovery to flow back to the ratio of the weight of the organic volatile in the weight of receipts (S7) and feed-in (S1) separator in this gas in bottom for this organic volatile.Namely in S7 the weight of this organic substance divided by the weight of this organic substance in S1.The ratio of the computational methods of the 3-picoline rate of recovery to be this organic volatile in overhead stream the collect weight of the organic volatile in the weight of (S3) and feed-in (S1) separator in this gas.
Comparative example 4-prior art condensation method
By high-temperature gas feed-in one condenser described in embodiment 7, be directly condensed into the liquid of 10 DEG C, become liquid at the bottom of tower, concentrate DMAc 58.2wt%, liquid dimethylacetylamide (DMAc) rate of recovery 92.5% at the bottom of tower, comparatively embodiment 7 is low.And in concentrate, the concentration of organic volatile is on the low side, because this increasing the energy cost of subsequent purification process organic volatile.Another part is uncondensed gas is then exhaust (tail gas), in exhaust, the concentration 890ppm of organic volatile dimethylacetylamide (DMAc), the concentration 124ppm of 3-MP, still need process with scrubbing tower, and a large amount of acid/neutralizing treatment liquid need be added thus consume energy, consume cost during washing.
Comparative example 5-prior art absorption process
By the high-temperature gas described in embodiment 7 by bottom feed-in one absorption tower, and add absorbent (water) in top, 180kg/hr, liquid at the bottom of tower, concentrate dimethylacetylamide (DMAc) 78.5wt%, dimethylacetylamide (DMAc) rate of recovery 95.6, comparatively embodiment 7 is low.And in concentrate, the concentration of organic volatile is on the low side, because this increasing the energy cost of subsequent purification process organic volatile.Another part is uncondensed gas is then exhaust (tail gas), in exhaust, the concentration 369ppm of the concentration 500ppm of organic volatile DMAc, 3-MP, still need process with scrubbing tower, and a large amount of acid/neutralizing treatment liquid need be added thus consume energy, consume cost during washing.
Above-described embodiment 7 and comparative example 4 and 5 as shown in table 3 below.
Table 2
Note: the label (S2, S3, S6, S7, D1 etc.) in form is applicable to embodiment and reference Figure 1B/3B.
Table 3
Note: the label (S2, S3, S6, S7, D1 etc.) in form is applicable to embodiment and reference Fig. 2 B/4B.
The condensation method of prior art, the condensation rate of recovery is on the low side, and organic volatile substrate concentration in its condensate liquid is also on the low side, thus adds the power consumption of subsequent purification process.Moreover the tail gas after its process, usually still containing certain density organic volatile, thus improves energy consumption, consumption cost during follow-up washing tail gas.
And the absorption process of prior art, not only need additionally to add absorbent/washing agent, altogether solidifying agent etc., and suitable absorbent need be selected for the organic volatile for reclaiming, thus restriction is caused to its application.Moreover, use absorbent to need the reproducer carrying out consuming energy, and a large amount of waste liquid can be caused to produce, disadvantageously increase running cost.Again, absorbent adds the corrosion to equipment, adversely affects absorption efficiency and exhaust-gas treatment ability after absorbing the organic substance in waste gas.Further, use water as absorbent/washing agent, also make the organic volatile substrate concentration that reclaims in liquid at the bottom of tower on the low side, cause the energy consumption improving subsequent purification process.In addition, the absorption of prior art, condensation technology, be only suitable for and reclaim high boiling organic volatile, effectively cannot reclaim the organic volatile of high and low boiling point simultaneously.
Relative to prior art, by gas processing method of the present invention, the rate of recovery of organic volatile is higher; And organic volatile substrate concentration in product stream is higher, and organic volatile substrate concentration in tail gas is lower, can improve the defect of prior art.Separately, gas processing method of the present invention, does not need additionally to add absorbent/solidifying agent, adsorbent altogether, and the material that separable acquisition gas mid-boiling point is higher and boiling point is lower.
In addition, relative to prior art, by gas handling system of the present invention, the rate of recovery of organic volatile is higher; And organic volatile substrate concentration in product stream is higher, and organic volatile substrate concentration in tail gas is lower, can avoid the defect of prior art.Separately, gas handling system of the present invention, does not need additionally to add absorbent/solidifying agent, adsorbent altogether.And by gas handling system of the present invention, the material that separable acquisition gas mid-boiling point is higher and boiling point is lower.
Above-described embodiment is illustrative gas processing method and gas handling system only, but not for limiting this exposure.These those skilled in the art any all without prejudice under spirit of the present invention and category, can carry out modifying to above-described embodiment and change.Therefore, the scope of the present invention, should be as contained in claims.
Claims (16)
1. a gas processing method, comprising:
By this gas containing organic volatile from load point feed-in separator to be separated; And
Above this load point, obtain the overhead stream containing the lower material of boiling point, obtain the bottom stream containing the higher material of boiling point below this load point, wherein, the backflow of this overhead stream of a part contacts with this gas in this separator.
2. gas processing method as claimed in claim 1, it is characterized in that, be this this separator of gas feed-in of 50 DEG C to 250 DEG C by temperature.
3. gas processing method as claimed in claim 1, it is characterized in that, reflux ratio is 0.1 to 100.
4. gas processing method as claimed in claim 1, it is characterized in that, this organic volatile is selected from by dimethylacetylamide, acetic acid, METHYLPYRROLIDONE, dimethyl formamide, pyridine, 3-picoline, propylene glycol monomethyl ether, propylene glycol monomethyl ether acetate, dimethyl sulfoxide (DMSO), ethyl acetate, ethylene glycol, diethylene glycol, triethylene glycol, propane diols, 1, 4-butanediol, diethylene glycol monobutyl ether, MEA, ethylenediamine, acrylic acid, methacrylic acid, glycol monoethyl ether, ethylene glycol monoethyl ether, dioxane, butanols, 2-butanols, isobutanol, 1, 4-butanediol, at least one in terpineol and alcohol ester 12 composition groups.
5. gas processing method as claimed in claim 1, is characterized in that, a part bottom this stream return this separator.
6. gas processing method as claimed in claim 1, is characterized in that, a part returns this separator after flowing through heat exchange bottom this.
7. gas processing method as claimed in claim 1, it is characterized in that, this load point is positioned at this separator bottom.
8. gas processing method as claimed in claim 1, it is characterized in that, this gas feed-in separator is to be separated this organic volatile by rectifying.
9. gas processing method as claimed in claim 1, it is characterized in that, the material that this boiling point is higher is selected from by dimethylacetylamide, acetic acid, METHYLPYRROLIDONE, dimethyl formamide, pyridine, 3-picoline, propylene glycol monomethyl ether, propylene glycol monomethyl ether acetate, dimethyl sulfoxide (DMSO), ethyl acetate, ethylene glycol, diethylene glycol, triethylene glycol, propane diols, 1, 4-butanediol, diethylene glycol monobutyl ether, MEA, ethylenediamine, acrylic acid, methacrylic acid, glycol monoethyl ether, ethylene glycol monoethyl ether, dioxane, butanols, 2-butanols, isobutanol, 1, 4-butanediol, at least one in terpineol and alcohol ester 12 composition groups.
10. a gas handling system, is characterized in that, comprising:
Separator, comprises packed bed and the load point in order to this gas of feed-in, and this load point is positioned at this separator bottom, it is characterized in that, this this separator of gas feed-in is separated, and to obtain overhead stream above this load point, obtains bottom stream below this load point; And
Heat exchanger, for the gaseous substance in this separator of condensation to obtain this overhead stream, and the backflow of this overhead stream of a part is to contact with this gas in this separator.
11. gas handling systems as claimed in claim 10, is characterized in that, are this gas feed-in separator of 50 DEG C to 250 DEG C by temperature.
12. gas handling systems as claimed in claim 10, it is characterized in that, this separator is rectifier unit.
13. gas handling systems as claimed in claim 10, it is characterized in that, this separator comprises one or more packed bed.
14. gas handling systems as described in claim 10, it is characterized in that, this heat exchanger is condenser.
15. gas handling systems as claimed in claim 10, is characterized in that, a part this bottom stream return this separator.
16. gas handling systems as claimed in claim 15, also comprise another heat exchanger, its for cool a part this bottom flow.
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