CN203447939U - Gas processing device - Google Patents
Gas processing device Download PDFInfo
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- CN203447939U CN203447939U CN201320397550.2U CN201320397550U CN203447939U CN 203447939 U CN203447939 U CN 203447939U CN 201320397550 U CN201320397550 U CN 201320397550U CN 203447939 U CN203447939 U CN 203447939U
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Abstract
The utility model provides a gas processing device. The gas processing device can utilize adsorbents to absorb and desorb gases containing organic solvents efficiently and continuously. The gas processing device is provided with a processed gas inlet pipeline (32), an adsorption tank (29) for preprocessing and a reflux gas pipeline (28), wherein the processed gas inlet pipeline is used for importing gases to be treated; the adsorption tank for preprocessing is arranged on the processed gas inlet pipeline (32) and is used for containing an adsorbent (30) for preprocessing; the reflux gas pipeline enables reflux gases generated by extruding desorbed gases from a condenser and/or a separator to return to the upstream side of the adsorption tank (29) for preprocessing on the processed gas inlet pipeline (32).
Description
Technical field
The utility model relates to a kind of gas treatment equipment, and it can carry out simultaneously: the operation of utilizing adsorbent to adsorb organic solvent contained in the gas that contains organic solvent, and the operation of adsorbed organic solvent being carried out to desorb.
Background technology
In recent years, the restriction of the concentration of emission of harmful Air Pollutants is progressively strengthened, the concentration this point that reduces the waste gas discharging from gas treatment equipment enjoys people to expect.
In the past, gas treatment equipment has following structure: be wherein provided with adsorbent adsorb 1 pair of adsorption tank of the organic solvent in processed gas, feedway from processed gas to each adsorption tank and the solution of supplying with smokes gas supply device, be also provided with and smoke the device switching between the desorption step of gas supplying with the absorption process of processed gas to adsorption tank and supply with solution.
As one of the adsorbent of gas treatment equipment example, use NACF (Activated Carbon Fiber(ACF), below, be recited as ACF).ACF has the performance of the gas of the organic solvent that good absorption contains low concentration, since ancient times, as adsorbent, uses.For example, propose following scheme in Japanese documentation JP 51-38278 communique (patent documentation 1), that is, ACF is fixed on supporter, or pass through self-sustained and form cylindricly, and be longitudinally fitted to the gas treatment equipment in core.
In addition, in the real fair 7-2028 communique (patent documentation 2) of Japanese documentation, the real fair 7-2029 communique (patent documentation 3) of Japanese documentation, the real fair 7-2030 communique of Japanese documentation (patent documentation 4), same absorption and desorption device has also been proposed.These are all to the core ejection steam that contains ACF, and desorption absorption is in the organic solvent of ACF.
[patent documentation 1] Japanese documentation JP 51-38278 communique
The real fair 7-2028 communique of [patent documentation 2] Japanese documentation
The real fair 7-2029 communique of [patent documentation 3] Japanese documentation
The real fair 7-2030 communique of [patent documentation 4] Japanese documentation
Utility model technical problem to be solved
With respect to the pore that participates in absorption, granular active carbon is macrovoid, and ACF is micropore, so ACF is very fast to the absorption of organic solvent and desorption rate, and completes at short notice desorb, is therefore a kind of well behaved recovery solvent.
In addition, if adsorbent is carried out to desorb with water vapour, the humidity once adsorbent becomes, wants to maintain absorption property in long time running, just must before upper once desorb, dry adsorbent.If this oven dry is abundant not,, along with the carrying out of running, the moist part of adsorbent can spread gradually, thereby significantly reduces absorption property.Compare with granular active carbon, ACF can be dried very rapidly, and therefore, generally, absorption process carries out with oven dry simultaneously.
Yet, along with the increase of organic solvent concentration in processed gas, also will increase with the weight of processing the corresponding adsorbent of air quantity, therefore in absorption process, dry the comparatively difficulty that becomes, so taked following various countermeasure simultaneously.
(1) baking operation is set separately: this countermeasure need to increase by 1 oven dry adsorption tank, this will make gas treatment equipment maximize, and it is complicated that treatment system becomes.
(2) improve the front temperature of absorption of processed gas: this countermeasure, along with the raising of adsorption temp, can reduce adsorption efficiency.
(3) reduce the front relative humidity of absorption of processed gas: this countermeasure need to be removed the auxiliary equipment of moisture.
(4) dilute processed gas and increase air quantity: this countermeasure is because the organic solvent concentration of absorption reduces, so adsorption efficiency also reduces.
Even if taked above-mentioned countermeasure, at absorption process initial stage of absorption process particularly, abundant not owing to drying, adsorbent humidity and high temperature, the adsorption capacity of adsorbent is recovered not yet completely, so organic solvent leaks in processed gas sometimes.
In addition, from the gap of the department of assembly of adsorbent and gap that filling produces, although only have denier but the leakage of processed gas can occur, therefore the removal capacity in only having the absorption process of 1 grade is 98～99% to have reached capacity, want further to improve removal capacity, just must take the multistage suction type of series connection.
In addition, the desorption gas by the desorb of desorption step institute carries out cooling with condenser, and then by separator, carries out separation recovery as reclaiming solvent.In condenser and/or separator, in order to prevent that pressure from increasing, and need to partially open the gas phase of condenser and/or separator.
Yet, the gas being trapped in condenser and/or separator of being extruded by desorption gas is the gas that contains the unconcentrated high levels of organic solvents close with saturated vapor pressure, therefore, need to attach oxidation Decomposition equipment and the reclaimer of the gas that set handling contains high levels of organic solvents.Below, the gas that contains high levels of organic solvents being trapped in condenser and/or separator of being extruded by desorption gas is called to " reflux gas ".Particularly, in the series multistage suction type of the removal capacity of having relatively high expectations, the processing completely of " reflux gas " is absolute condition.
In the starting stage of desorption step, the processed gas being trapped in adsorption tank is extruded to condenser and/or separator by stripping steam.But, because whole processed gas almost is not condensed, therefore, only have " reflux gas " of the volume part of about adsorption tank to be discharged at short notice.After this, the steam that contains organic solvent being almost all condensed is admitted to condenser and/or separator, and therefore the air quantity of " reflux gas " will obviously reduce.
That is, the air quantity of " reflux gas " reaches maximum at the desorption step initial stage, after this obviously reduce, so the organic solvent that high efficiency reclaims in " reflux gas " is comparatively difficult.
In addition, from environmental protection and the angle that reduces production costs, consider, can re-use under many circumstances the separated organic solvent reclaiming, therefore in order to improve the rate of recovery, need to effectively reclaim " reflux gas " that contains high levels of organic solvents.
Therefore, the purpose of this utility model is the gas processing method that a kind of gas treatment equipment is provided and utilizes this gas treatment equipment, and it can utilize adsorbent efficiently and continuously to carry out the absorption and desorption of the gas to containing organic solvent.
Utility model content
Be accompanied by the raising to environmental awareness in recent years, to the restriction of organic solvent content in emission gases also day by day strengthening, therefore reducing organic solvent content is trend of the times.In the situation that the organic solvent concentration of processed gas is higher, require removal capacity to reach more than 99%, therefore adopt the situation of series multistage suction type in continuous increase.
Order as series multistage suction type, using the 1st grade of operation of at first processed gas being carried out to adsorption treatment as the 1st absorption process, after this, the raising along with treatment effeciency has increased absorption process 2nd grade (2nd absorption process), the 3rd level (3rd absorption process) connected in series with processing path.
In addition, in order not reduce desorption efficiency, desorption step the 1st grade of adsorption treatment the 1st absorption process after finishing, be advisable, the 2 grades of suction types of serial of take are example, and the processing in specific adsorption tank repeats as good according to the circular order of desorption step → 2nd absorption process → 1st absorption process → desorption step.
The utility model is in series multistage suction type, previous stage setting at processed gas supply part is filled with the pretreatment adsorption tank of adsorbent for pretreatment, and be provided with the reflux gas of being extruded by desorption gas is delivered to the previous stage of adsorption tank for pretreatment, and after mixing with processed gas, the device that makes it use adsorption tank by pretreatment and process in the 1st grade of adsorption tank, thereby can make the variation of the absorption process inlet gas concentration that reflux gas causes mild, therefore can prevent that degraded and the performance of adsorbing the caused adsorbent of heat from reducing.In addition, the purpose of this utility model is also to provide a kind of gas treatment equipment, and it is compared when processing reflux gas with other treatment facilities, can reclaim more efficiently organic solvent, than in the past more small-sized, also reduced operation cost.
Gas treatment equipment of the present utility model, there is the adsorbent that can adsorb organic solvent, and there is processed gases that at least 3 above alternative supplies contain organic solvent and treatment trough for the heating steam from described adsorbent desorb organic solvent, described gas treatment equipment also possesses: heating steam supply unit, and it imports described heating steam to a described treatment trough of selecting from a plurality of described treatment troughs; Processed gas supply part, it passes through the remaining a plurality of described treatment troughs of plural serial stage, and imports described processed gas to a plurality of described treatment trough of plural serial stage; Recovering mechanism portion, it has the gas phase portion being connected with described heating steam supply unit, and is included in condenser and/or the separator that reclaims organic solvent while supplying with described heating steam from the desorption gas of described treatment trough discharge.
Described processed gas supply part has: process gas access pipeline, it imports above-mentioned processed gas; Pretreatment adsorption tank, it is arranged at above-mentioned processing gas access pipeline, and receives pretreatment adsorbent.
Described recovering mechanism portion has reflux gas pipeline, and it makes the reflux gas of being extruded from above-mentioned condenser and/or separator by above-mentioned desorption gas turn back to the upstream side of adsorption tank for the pretreatment of above-mentioned processing gas access pipeline.
In 1 embodiment, above-mentioned adsorbent is NACF or granular active carbon.
In 1 embodiment, above-mentioned pretreatment is at least one of granular active carbon, NACF, zeolite, silica gel, ion exchange resin and activated alumina group with adsorbent.
Gas processing method of the present utility model, from the processed gas that contains organic solvent, reclaim organic solvent, it utilizes according to the gas treatment equipment described in above-mentioned any 1, the above-mentioned reflux gas of being extruded from above-mentioned condenser and/or separator by above-mentioned desorption gas is mixed with above-mentioned processed gas, to with the above-mentioned desorption gas after adsorption tank, from above-mentioned processed gas supply part, import a plurality of described treatment troughs of residue of series connection by above-mentioned pretreatment, and reclaiming organic solvent from the processed gas that contains organic solvent.
Utility model effect
By based on gas treatment equipment of the present utility model and the gas processing method that utilizes this gas treatment equipment, can utilize adsorbent efficiently and continuously the gas that contains organic solvent to be carried out to absorption and desorption.
Accompanying drawing explanation
Fig. 1 shows the formation of gas treatment equipment of the present embodiment and the key diagram of the 1st operation that utilizes the gas processing method of this gas treatment equipment;
Fig. 2 is the key diagram that shows the 2nd operation of the gas processing method that utilizes in the present embodiment gas treatment equipment;
Fig. 3 is the key diagram that shows the 3rd operation of the gas processing method that utilizes in the present embodiment gas treatment equipment.
Symbol description
1 pressure fan
2 the 1st treatment troughs
3 the 2nd treatment troughs
4 the 3rd treatment troughs
5A the 1st adsorbent
5B the 2nd adsorbent
5C the 3rd adsorbent
6 the 1st automatic upper wind doors
7 the 2nd automatic upper wind doors
8 the 3rd automatic upper wind doors
9 the 1st automatic lower wind doors
10 the 2nd automatic lower wind doors
11 the 3rd automatic lower wind doors
12 the 1st derive open and close valve
13 the 3rd derive open and close valve
14 the 5th derive open and close valve
15 the 2nd derive open and close valve
16 the 4th derive open and close valve
17 the 6th derive open and close valve
18 the 2nd import open and close valve
19 the 4th import open and close valve
20 the 6th import open and close valve
21 the 1st import open and close valve
22 the 3rd import open and close valve
23 the 5th import open and close valve
24 desorption gas pipelines
25 condensers
26 reclaim liquid pipeline
27 separators
27A liquid phase region
27B gas phase zone
27C recovery line
28 reflux gas pipelines
29 pretreatment adsorption tanks
30 pretreatment adsorbents
31 process gas introduction tube line
31A the 1st take-off line
31B the 1st processes gas introduction tube line
31C the 1st diluent gas imports pipeline
31D the 2nd take-off line
31E the 2nd processes gas introduction tube line
31F the 2nd diluent gas imports pipeline
31G the 3rd take-off line
31H the 3rd processes gas introduction tube line
31I the 3rd diluent gas imports pipeline
31J the 1st derives pipeline
31K the 2nd derives pipeline
31L the 3rd derives pipeline
31M the 4th derives pipeline
31N the 5th derives pipeline
31P the 6th derives pipeline
32 process gas access pipeline
34 heating steam feedwaies
35 heating steam pipelines
35A the 1st heating steam take-off line
35B the 2nd heating steam take-off line
35C the 3rd heating steam take-off line
36 the 1st steam open and close valves
37 the 2nd steam open and close valves
38 the 3rd steam open and close valves
100 gas treatment equipments.
The specific embodiment
Below, with reference to accompanying drawing, illustrate embodiment of the present utility model.In addition, in embodiment shown below, for identical or corresponding part, use in the drawings prosign, sometimes do not carry out repeat specification.In addition, in the embodiment of the following stated, while being mentioned to number, quantity etc., unless there is special records, scope of the present utility model might not be subject to the restriction of its number, quantity etc.
The organic solvent that used in this manual refers to: chloromethanes, chloroform, carbon tetrachloride, vinyl chloride, trichloro-ethylene, tetrachloro-ethylene, o-dichlorohenzene, m-dichlorobenzene, F-11 2, F-11 3, HCFC, HFC, propyl bromide, butyl iodide, methyl acetate, ethyl acetate, n-propyl acetate, butyl acetate, vinyl acetate, methyl propionate, methyl acrylate, ethyl acrylate, butyl acrylate, methyl methacrylate, diethyl carbonate, Ethyl formate, ether, dipropyl ether, oxolane, butyl ether, methyl phenyl ethers anisole, methyl alcohol, ethanol, isopropyl alcohol, n-butanol, sec-butyl alcohol, isobutanol, the tert-butyl alcohol, allyl alcohol, amylalcohol, enanthol, ethylene glycol, diethylene glycol (DEG), phenol, orthoresol, metacresol, paracresol, xylenol, acetone, methyl ethyl ketone, methyl iso-butyl ketone (MIBK), cyclohexanone, phorone, acrylonitrile, n-hexane, isohexane, cyclohexane, hexahydrotoluene, normal heptane, normal octane, positive nonane, isononane, decane, dodecane, hendecane, the tetradecane, decahydronaphthalene, benzene, toluene, meta-xylene, paraxylene, ortho-xylene, ethylbenzene, 1,3,5-trimethylbenzene, 1-METHYLPYRROLIDONE, dimethyl formamide, dimethylacetylamide and dimethyl sulfoxide (DMSO) etc.
(gas treatment equipment 100)
With reference to Fig. 1, the formation of the gas treatment equipment 100 of the present embodiment is described.Fig. 1 is the key diagram of formation that shows the gas treatment equipment 100 of the present embodiment.This gas treatment equipment 100, is configured to and can realizes the multistage suction type of serial, and possesses the 1st treatment trough the 2, the 2nd treatment trough 3 and the 3rd treatment trough 4.
The 1st treatment trough 2 comprises the 1st adsorbent 5A of drum, and the 2nd treatment trough 3 comprises the 2nd adsorbent 5B of drum, and the 3rd treatment trough 4 comprises the 3rd adsorbent 5C of drum.The 1st adsorbent 5A, the 2nd adsorbent 5B and the 3rd adsorbent 5C, processed gas outside-in is by implementing absorption process, and heating steam is from inner side laterally by implementing desorption step.The 1st adsorbent 5A, the 2nd adsorbent 5B and the 3rd adsorbent 5C are all used ACF.
The 1st treatment trough the 2, the 2nd treatment trough 3 and the 3rd treatment trough 4 are connected with processing gas introduction tube line 31 and desorption gas pipeline 24.For carry out with process the switching being communicated with between gas introduction tube line 31 and with desorption gas pipeline 24 between the switching being communicated with, on the 1st treatment trough the 2, the 2nd treatment trough 3 and the 3rd treatment trough 4, be provided with respectively the 1st automatic lower wind door 9, the 2nd automatic lower wind door 10 and the 3rd automatic lower wind door 11.
On the 1st take-off line 31A of the 1st 2 branches for the treatment of trough that processes gas introduction tube line 31, be provided with the 1st and import open and close valve 21, the 1st processes gas introduction tube line 31B is connected with the 1st take-off line 31A, and the 1st diluent gas imports pipeline 31C and the 1st processing gas introduction tube line 31B is connected.The 1st, process on gas introduction tube line 31B, be provided with the 2nd and import open and close valve 18.
On the 2nd take-off line 31D of the 2nd 3 branches for the treatment of trough that processes gas introduction tube line 31, be provided with the 3rd and import open and close valve 22, the 2nd processes gas introduction tube line 31E is connected with the 2nd take-off line 31D, and the 2nd diluent gas imports pipeline 31F and the 2nd processing gas introduction tube line 31E is connected.The 2nd, process on gas introduction tube line 31E, be provided with the 4th and import open and close valve 19.
On the 3rd take-off line 31G of the 3rd 4 branches for the treatment of trough that processes gas introduction tube line 31, be provided with the 5th and import open and close valve 23, the 3rd processes gas introduction tube line 31H is connected with the 3rd take-off line 31G, and the 3rd diluent gas imports pipeline 31I and the 3rd processing gas introduction tube line 31H is connected.The 3rd, process on gas introduction tube line 31H, be provided with the 6th and import open and close valve 20.
Above the 1st treatment trough 2, the 1st automatic upper wind door 6, the 1st that is provided with the circulation of controlling processed gas is derived pipeline 31J and the 2nd derivation pipeline 31K.The 1st, derive on pipeline 31J, be provided with the 1st and derive open and close valve 12, and derive on pipeline 31K the 2nd, be provided with the 2nd and derive open and close valve 15.
Above the 2nd treatment trough 3, the 2nd automatic upper wind door 7, the 3rd that is provided with the circulation of controlling processed gas is derived pipeline 31L and the 4th derivation pipeline 31M.The 3rd, derive on pipeline 31L, be provided with the 3rd and derive open and close valve 13, and derive on pipeline 31M the 4th, be provided with the 4th and derive open and close valve 16.
Above the 3rd treatment trough 4, the 3rd automatic upper wind door 8, the 5th that is provided with the circulation of controlling processed gas is derived pipeline 31N and the 6th derivation pipeline 31P.The 5th, derive on pipeline 31N, be provided with the 5th and derive open and close valve 14, and derive on pipeline 31P the 6th, be provided with the 6th and derive open and close valve 17.
The 1st heating steam take-off line 35A branching out from heating steam pipeline 35 is connected with the 1st treatment trough 2, and is provided with the 1st steam open and close valve 36 on the 1st heating steam take-off line 35A.The 2nd heating steam take-off line 35B branching out from heating steam pipeline 35 is connected with the 2nd treatment trough 3, and is provided with the 2nd steam open and close valve 37 on the 2nd heating steam take-off line 35B.The 3rd heating steam take-off line 35C branching out from heating steam pipeline 35 is connected with the 3rd treatment trough 4, and is provided with the 3rd steam open and close valve 38 on the 3rd heating steam take-off line 35C.
In addition, in above-mentioned gas treating apparatus 100, the 1st automatic upper wind door 6, the 2nd automatic upper wind door 7, the 3rd automatic upper wind door 8, the 1st automatic lower wind door 9, the 2nd automatic lower wind door 10, the 3rd automatic lower wind door 11, the 1st imports open and close valve 21, the 2nd imports open and close valve 18, the 3rd imports open and close valve 22, the 4th imports open and close valve 19, the 5th imports open and close valve 23, the 6th imports open and close valve 20, the 1st derives open and close valve 12, the 2nd derives open and close valve 15, the 3rd derives open and close valve 13, the 4th derives open and close valve 16, the 5th derives open and close valve 14, the 6th derives open and close valve 17, heating steam feedway 34, the 1st steam open and close valve 36, the 2nd steam open and close valve 37, the 3rd steam open and close valve 38, condenser 25, separator 27 and pressure fan 1, by not shown control device, suitably control running and open and close, to be achieved as follows described gas processing method.
In addition, in above-mentioned gas treating apparatus 100, at least by heating steam feedway 34, the 1st heating steam take-off line 35A, the 1st steam open and close valve the 36, the 2nd heating steam take-off line 35B, the 2nd steam open and close valve the 37, the 3rd heating steam take-off line 35C and the 3rd steam open and close valve 38, form heating steam supply unit.
In addition, at least by pressure fan 1, process gas access pipeline 32, process gas introduction tube line 31, the 1st take-off line 31A, the 1st processes gas introduction tube line 31B, the 1st diluent gas imports pipeline 31C, the 2nd imports open and close valve 18, the 1st imports open and close valve 21, the 2nd take-off line 31D, the 2nd processes gas introduction tube line 31E, the 2nd diluent gas imports pipeline 31F, the 4th imports open and close valve 19, the 3rd imports open and close valve 22, the 3rd take-off line 31G, the 3rd processes gas introduction tube line 31H, the 3rd diluent gas imports pipeline 31I, the 6th imports open and close valve 20 and the 5th imports the processed gas supply part of open and close valve 23 formation.
In addition, at least by desorption gas pipeline 24, condenser 25, recovery liquid pipeline 26, separator 27 and recovery line 27C, form recovering mechanism portion.
(gas processing method)
Below, referring to figs. 1 through Fig. 3, to using the gas processing method of the gas treatment equipment 100 with above-mentioned formation to describe.Fig. 1 to Fig. 3 is the 1st key diagram to the 3rd operation that shows the gas processing method that uses in the present embodiment gas treatment equipment 100.
In the 1st operation shown in Fig. 1, the 1st treatment trough 2 of gas treatment equipment 100 is implemented the 1st absorption process, and the 2nd treatment trough 3 is implemented the 2nd absorption process, and the 3rd treatment trough 4 is implemented desorption step.
In the 2nd operation shown in Fig. 2, the 1st treatment trough 2 of gas treatment equipment 100 is implemented desorption step, and the 2nd treatment trough 3 is implemented the 1st absorption process, and the 3rd treatment trough 4 is implemented the 2nd absorption process.
In the 3rd operation shown in Fig. 3, the 1st treatment trough 2 of gas treatment equipment 100 is implemented the 2nd absorption process, and the 2nd treatment trough 3 is implemented desorption step, and the 3rd treatment trough 4 is implemented the 1st absorption process.
< the 1st operation >
(the 1st absorption process of the 1st treatment trough 2)
According to Fig. 1, the processed gas A that comprises the gas that contains organic solvent, the 1st treatment trough 2 of sending in the 1st absorption process from processing gas access pipeline 32 by pressure fan 1.The 1st automatic lower wind door 9, controls the opening of the 1st take-off line 31A and closing of desorption gas pipeline 24.
The 1st automatic upper wind door 6 is controlled as the negotiable open state of processed gas A making in the 1st adsorbent 5A.In addition, the 1st imports open and close valve 21 is controlled as open state, and the 3rd importing open and close valve 22 and the 5th importing open and close valve 23 are controlled as closed condition.
The 1st adsorbent 5A by the 1st treatment trough 2 carries out gas absorption, and derive pipeline 31K as the 1st absorption process exit gas B from the 2nd, derives.The 2nd derives open and close valve 15 is controlled as open state, and the 1st derivation open and close valve 12 is controlled as closed condition.In addition, the 1st steam open and close valve 36 of the 1st heating steam take-off line 35A is controlled as closed condition.
(the 2nd absorption process of the 2nd treatment trough 3)
Owing to containing the organic solvent leaking out in the 1st absorption process in the 1st absorption process exit gas B, for further carrying out adsorption treatment, connected in series with the 2nd treatment trough 3 in the 2nd absorption process, as the 2nd absorption inlet gas C, will be admitted to the 2nd and process gas introduction tube line 31E.The 2nd automatic lower wind door 10, controls the opening of the 2nd take-off line 31D side and closing of desorption gas pipeline 24.
Now, in the 2nd absorption process, in order to impel the 2nd adsorbent 5B of the 2nd treatment trough 3 dry, in the 2nd absorption inlet gas C, sneak into air quantity by the controlled diluent gas L of the 2nd diluent gas importing pipeline 31F.The 4th imports open and close valve 19 is controlled as open state.
So-called diluent gas L refers in the absorption process after the 2nd absorption process in order to impel the dry and gas that appends of adsorbent, it can comprise extraneous air, for instrument air, nitrogen and argon gas any one and form.
The 2nd absorption inlet gas C is undertaken, after adsorption treatment, becoming pure air D by the 2nd adsorbent 5B in the 2nd treatment trough 3, derives pipeline 31L derive to the outside of gas treatment equipment 100 from the 3rd.The 2nd automatic upper wind door 7 is controlled as and makes the absorption of the 2nd in the 2nd adsorbent 5B inlet gas C in negotiable open state.In addition, the 3rd derives open and close valve 13 is controlled as open state, and the 4th derives open and close valve 16 is controlled as closed condition.In addition, the 2nd steam open and close valve 37 of the 2nd heating steam take-off line 35B is controlled as closed condition.
(desorption step of the 3rd treatment trough 4)
In the 1st operation, needn't send into processed gas to the 3rd treatment trough 4, and be controlled so as to that the 3rd take-off line 31G closes and the open state of desorption gas pipeline 24 by the 3rd automatic lower wind door 11.In addition, the 3rd automatic upper wind door 8, close gas from inner side, the lateral circulation of the 3rd adsorbent 5C, and smoke heating steam by the 3rd heating steam take-off line 35C from the solution of heating steam feedway 34, from the inner side of the 3rd adsorbent 5C, be fluidly imported into laterally.The 3rd steam open and close valve 38 of the 3rd heating steam take-off line 35C is controlled as open state.
In the 3rd treatment trough 4, ejection heating steam, and be desorbed by the 3rd adsorbent 5C by the organic solvent of the 3rd adsorbent 5C absorption.The organic solvent gas being desorbed is admitted in condenser 25 after by desorption gas pipeline 24.
The organic solvent gas being desorbed and heating steam condensation in condenser 25, the condensate liquid that contains high levels of organic solvents is sent into separator 27 by reclaiming liquid pipeline 26.Condensate liquid is separated into organic solvent and water in separator 27, reclaims solvent K and is recovered by recovery line 27C.
Be trapped in the reflux gas in condenser 25 and separator 27, by desorption gas, be extruded, and import to and process in gas access pipeline 32 by reflux gas pipeline 28, mix with processed gas A.
The processed gas A and the reflux gas that from processing gas access pipeline 32, import, send in the 1st treatment trough 2 with after processing in adsorption tank 29 in pretreatment.In the 1st operation, repeat above-mentioned operation, reclaim solvent K and be recovered from recovery line 27C.
< the 2nd operation >
According to Fig. 2, in the 2nd operation, in the 1st treatment trough 2 of gas treatment equipment 100, implement desorption step, in the 2nd treatment trough 3, implement the 1st absorption process, and in the 3rd treatment trough 4, in order to implement the 2nd absorption process, by not shown control device, suitably control the 1st automatic upper wind door 6, the 2nd automatic upper wind door 7, the 3rd automatic upper wind door 8, the 1st automatic lower wind door 9, the 2nd automatic lower wind door 10, the 3rd automatic lower wind door 11, the 1st imports open and close valve 21, the 2nd imports open and close valve 18, the 3rd imports open and close valve 22, the 4th imports open and close valve 19, the 5th imports open and close valve 23, the 6th imports open and close valve 20, the 1st derives open and close valve 12, the 2nd derives open and close valve 15, the 3rd derives open and close valve 13, the 4th derives open and close valve 16, the 5th derives open and close valve 14, the 6th derives open and close valve 17, condenser 25, separator 27, pressure fan 1, heating steam feedway 34, the 1st heating steam take-off line 35A, the 1st steam open and close valve 36, the 2nd heating steam take-off line 35B, the 2nd steam open and close valve 37, the running of the 3rd heating steam take-off line 35C and the 3rd steam open and close valve 38, the switching of each open and close valve is switched.
< the 3rd operation >
According to Fig. 3, in the 3rd operation, in the 1st treatment trough 2 of gas treatment equipment 100, implement the 2nd absorption process, in the 2nd treatment trough 3, implement desorption step, and in the 3rd treatment trough 4, in order to implement the 1st absorption process, by not shown control device, suitably control the 1st automatic upper wind door 6, the 2nd automatic upper wind door 7, the 3rd automatic upper wind door 8, the 1st automatic lower wind door 9, the 2nd automatic lower wind door 10, the 3rd automatic lower wind door 11, the 1st imports open and close valve 21, the 2nd imports open and close valve 18, the 3rd imports open and close valve 22, the 4th imports open and close valve 19, the 5th imports open and close valve 23, the 6th imports open and close valve 20, the 1st derives open and close valve 12, the 2nd derives open and close valve 15, the 3rd derives open and close valve 13, the 4th derives open and close valve 16, the 5th derives open and close valve 14, the 6th derives open and close valve 17, condenser 25, separator 27, pressure fan 1, heating steam feedway 34, the 1st heating steam take-off line 35A, the 1st steam open and close valve 36, the 2nd heating steam take-off line 35B, the 2nd steam open and close valve 37, the running of the 3rd heating steam take-off line 35C and the 3rd steam open and close valve 38, the switching of each open and close valve is switched.
As mentioned above, manage throughout cycle for the treatment of in groove control make desorption step → 2nd absorption process → 1st absorption process → desorption step circulation repeatedly, thereby in the gas treatment equipment 100 of the present embodiment, can to processed gas A, process continuously.
Like this, according to the gas treatment equipment 100 of the present embodiment, by series connection more than 2 grades in treatment trough, process the multistage suction type of serial that processed gas A contains the gas of organic solvent, can realize than 1 grade of clearance that suction type is higher.
In addition, according to the gas treatment equipment 100 of the present embodiment, reflux gas is sent into the previous stage of adsorption tank 29 for pretreatment, after mixing with processed gas A, make it by pretreatment adsorption tank 29, thereby can utilize pretreatment with adsorption tank 29, to remove the material that makes adsorbent degraded of being located in treatment trough.
The said material that makes adsorbent degraded here, refers to that boiling point is difficult to resolve suction material and oxidizing gas, polymerism material etc. at more than 200 ℃ high boiling substance etc.In addition, can also make the variation of the absorption process inlet gas concentration that reflux gas causes mild significantly.Accordingly, the caused thermal runaway of absorption heat occurring in the 1st grade of adsorption tank can be suppressed at, the degraded of adsorbent and the reduction of absorption property can also be prevented.
In addition, according to the gas treatment equipment 100 of the present embodiment, by making mixed being incorporated in the 1st grade for the treatment of trough of reflux gas and processed gas, again adsorb recycling, thereby compare with utilizing oxidation Decomposition equipment and reclaimer otherwise processed reflux gas, can access the higher organic efficiency to organic solvent.
Therefore in addition, according to the gas treatment equipment 100 of the present embodiment, do not need the equipment of otherwise processed reflux gas, can save taking up room of gas treatment equipment, than the gas treatment equipment in the past price that more can reduce production costs.
In addition, according to the gas treatment equipment 100 of the present embodiment, do not need the equipment of otherwise processed reflux gas, therefore more in the past than the operation cost price that more can reduce gas treatment equipment.
In addition, according to the gas treatment equipment 100 of the present embodiment, because process reflux gas in the 1st grade for the treatment of trough, make processed gas concentration increase, but the gas that contains organic solvent leaking out is adsorbed without any problems by the 2nd grade of adsorbent connected in series, therefore can process processed gas by the identical removal capacity of multistage suction type with the serial with in the past in the 1st absorption process.
The adsorbent that the gas treatment equipment 100 of the present embodiment is used, can be used ACF or granular active carbon.Said ACF here, can be by existing method to the serial fiber of polyacrylonitrile (PAN), artificial silk series, coal tar pitch is serial, phenolic resin is serial, asphalt is serial and the raw fibres such as series that derive from plant are processed resulting specific area 300～3000M2/G, fibre diameter is that 2 μ M～30 μ M left and right, fibre length are that 0.5MM～100MM left and right, average pore diameter are
~
the material of left and right.
Below, by enumerating embodiment, be described more specifically the gas treatment equipment 100 of the present embodiment.
< embodiment >
In an example of processed gas, the gas that contains organic solvent is chloromethanes, and adsorbent is used Japan to spin ACF " K-FILTER " the 3.8KG/ groove that Co., Ltd. produces, and one time the required quantity of steam of desorb is set as 1.9kg.
To contain chloromethanes 22, the processed gas of 25 ℃ of 000ppm, with air quantity 2.7Nm
3/ min blows in the 1st treatment trough 2 in the 1st absorption process by pressure fan 1.Then, using the 1st absorption process exit gas B of discharge from the 1st treatment trough 2 as the 2nd absorption inlet gas C, in the 2nd treatment trough 3 in the 2nd absorption process, blow.Now, the 2nd absorption inlet gas C is by 0.6Nm
3the extraneous air dilution of/min, temperature is adjusted to 40 ℃.After processing, as pure air, from the 3rd, derive pipeline 31L to system outside drain in the 2nd treatment trough 3.
When the chloromethanes concentration of the 1st absorption process exit gas B from the 1st treatment trough 2 discharges reaches 1,100ppm, carry out the switching of each operation.During the 1st treatment trough 2 carries out the 1st absorption process, in the 3rd treatment trough 4, spray stripping steam and carry out desorption step.
Desorption gas carries out condensation by condenser 25, and is separated into organic solvent and water by separator 27.The gas being trapped in condenser 25 and separator 27 is extruded by desorption gas, and sends into the processing gas access pipeline 32 of the previous stage of adsorption tank 29 for pretreatment after by reflux gas pipeline 28 as reflux gas.Pretreatment is used granular active carbon with the pretreatment of adsorption tank 29 with adsorbent 30.
Cycle for the treatment of in particular procedure groove, carries out according to the order of absorption process → 1st, desorption step → 2nd absorption process, usings absorption process → 1st, desorption step → 2nd absorption process as 1 circulation, implements altogether 8 circulations.8 cycle operation of take are 1 group, repeat 100 groups, implement the degraded of each treatment trough ACF and confirm.
< comparative example 1 >
Except pretreatment not being set in 2 grades of suction types of serial with adsorption tank 29, carry out same gas treatment with above-described embodiment, implemented the degraded of ACF and confirmed.
< comparative example 2 >
In 2 grades of suction types of serial, there is no reflux gas pipeline 28 and adsorption tank 29 for pretreatment, reflux gas utilizes oxidation Decomposition treating apparatus to carry out otherwise processed.In addition, carry out same gas treatment with above-described embodiment, implemented the degraded of ACF and confirmed.
< comparative example 3 >
The condition of processed gas, adsorbent, stripping vapor amount, carries out same setting with above-described embodiment, does not adopt 2 grades of suction types of serial and adopts 1 grade of suction type to implement gas treatment.The gas being trapped in condenser and separator of being extruded by desorption gas is delivered to pretreatment with before adsorption tank as reflux gas.Using absorption process → desorption step 2 operations as 1 time circulation, implement altogether 12 times circulation.Using 12 cycle operation as 1 group, repeat 66 groups, implemented the degraded of ACF and confirmed.
In the absorption process of embodiment, comparative example 1 to 3, use the analyzer of the total hydrocarbon meter of Shimadzu Seisakusho Ltd.'s production to measure the concentration of gas and the concentration of the 1st absorption process inlet gas from absorption process final outlet to system outside drain.
The BET specific area of the ACF before and after enforcement is confirmed in degraded, and the specific area pore measure of spread device (Gemini2375) that uses MicromeriticsJapan contract commercial firm to produce is measured.By ACF vacuum drying 12 hours under the condition of 120 ℃, in the scope that is 0.02～0.95 at relative pressure, measure the adsorbance of nitrogen in the boiling point (195.8 ℃) of liquid nitrogen, and draw the adsorption isotherm of sample.The result of take in the scope of relative pressure 0.02～0.15, as basis, is calculated according to BET method.
The pore diameter of the ACF before and after enforcement is confirmed in degraded
following micropore pore volume, the specific area pore measure of spread device (Gemini2375) that uses MicromeriticsJapan contract commercial firm to produce is measured.By ACF vacuum drying 12 hours under the condition of 120 ℃, in the scope that is 0.02～0.95 at relative pressure, measure the adsorbance of nitrogen in the boiling point (195.8 ℃) of liquid nitrogen, and draw the adsorption isotherm of sample.
Analytical range 0～
, t determines, under the condition of formula H.J, according to MP method, to resolve this result, the result of the micropore fine pore distribution number table during according to absorption deducts pore diameter and exists from the pore volume of full micropore
above micropore pore volume and calculating.
Table 1 is the explanation that shows the embodiment of the gas processing method that utilizes in the present embodiment gas treatment equipment and the result of comparative example.Table 1 show embodiment and the absorption process entrance of comparative example 1 to 3 and the chloromethanes concentration of outlet, circulation finish the rate of recovery of the isolated liquid chlorine methane of rear separator institute, repeat approximately 800 absorption and desorption circulate after the surface physical property of ACF.
The surface physical property of ACF before cycle operation: BET specific area is 1610m
2/ g,
following full micropore volume is 0.64m
3/ g.
Table 1
By table 1, can find out, according to the gas treatment equipment of the present embodiment and the gas processing method that utilizes this gas treatment equipment, there is 2 grades of suction types of serial and reflux gas, compare with the comparative example 1 of adsorption tank with pretreatment is not set, absorption process exit concentration and the chloromethanes rate of recovery are identical.
Yet, during the surface physical property of ACF is evaluated after repeating approximately 800 absorption and desorption circulation, in comparative example 1, found degraded, on the contrary, in the gas treatment equipment of the present embodiment, do not degrade completely obviously.This can be described as owing to making processed gas use adsorption tank to relax absorption entrance concentration by pretreatment, has therefore effectively suppressed the intensification by the ACF of the caused surplus of absorption heat.
The gas treatment equipment of the present embodiment, do not there is 2 grades of suction types of serial and reflux gas, compare with the comparative example 2 of adsorption tank with not having pretreatment, after repeating approximately 800 absorption and desorption circulation, the surface physical property of ACF is identical, does not find degraded completely.
In addition, although the average chloromethanes concentration of absorption outlet is also identical, the chloromethanes rate of recovery has obviously improved approximately 11.4%.This can say, the reflux gas pipeline 28 of the present embodiment and pretreatment have effectively improved the rate of recovery of organic solvent with adsorption tank 29.In addition, not recoverable chloromethanes 4.9% means dissolving or is dispersed in the amount in the water stratification in separator in an embodiment, therefore irrelevant with the discharge capacity to system outside.
Gas treatment equipment of the present utility model, there is 1 grade of suction type and reflux gas, compare with having the gas treatment equipment (comparative example 3) of pretreatment with adsorption tank, reduced significantly the average chloromethanes concentration of absorption outlet, liquid chlorine methane recovery has also obviously improved approximately 1.0%.
By above explanation, confirm: according to the gas treatment equipment of the present embodiment, by reflux gas pipeline and pretreatment adsorption tank are set in the multistage suction type of serial, there is the average removal rate and the rate of recovery that improve organic solvent, the effect of performance restrain adsorption agent degraded.
Above, according to the gas treatment equipment of the present embodiment and the gas processing method that utilizes this gas treatment equipment, reflux gas is sent into the previous stage of adsorption tank for pretreatment in the multistage suction type of serial, and after mixing with processed gas, make it use adsorption tank and process in the 1st grade of adsorption tank by pretreatment, by this method is set, not only can realize than installed higher clearance in the past, but also can be in pretreatment with removing the material that make adsorbent degraded in adsorption tank.
In addition, because the variation of the absorption process inlet gas concentration that can make reflux gas cause obtains gently significantly, therefore can prevent that degraded and the performance of the adsorbent that caused by absorption heat from reducing.In addition, by process reflux gas in the 1st grade of adsorption tank, can obtain the rate of recovery of higher organic solvent when processing with other treatment facility.Therefore in addition, owing to not needing reflux gas to carry out the equipment of otherwise processed, can provide than the more small-sized and cheaper gas treatment equipment of operation cost price in the past.
In addition, the gas treatment equipment 100 of above-described embodiment, in order to realize the multistage suction type of serial, 3 groove structures of the 1st treatment trough the 2, the 2nd treatment trough 3 and the 3rd treatment trough 4 have been adopted, and 2 grades of suction types of serial have been adopted, although repeat successively the method for the circulation of desorption step → 2nd absorption process → 1st absorption process → desorption step in groove is illustrated about managing throughout, but be not limited to 2 grades of suction types of serial, even if adopt the multistage suction types of serial such as 3 grades of suction types of serial, 4 grades of suction types of serial also can access same action effect.
This disclosed above-mentioned embodiment and embodiment, be example in all respects, do not limit the utility model.The utility model protection domain delimited by claims, and comprise with claim scope is recorded having all changes in same meaning and same range.
Claims (3)
1. a gas treatment equipment, it has the adsorbent that can adsorb organic solvent, and there is processed gases that at least 3 above alternative supplies contain organic solvent and treatment trough for the heating steam from described adsorbent desorb organic solvent, it is characterized in that possessing:
Heating steam supply unit, it imports described heating steam to a described treatment trough of selecting from a plurality of described treatment troughs;
Processed gas supply part, it is by the remaining a plurality of described treatment troughs of plural serial stage, to the described processed gas of a plurality of described treatment trough importing of plural serial stage;
Recovering mechanism portion, it has the gas phase portion being connected with described heating steam supply unit, and is included in condenser and/or the separator that reclaims organic solvent the desorption gas of discharging from described treatment trough while supplying with described heating steam,
Described processed gas supply part, has:
Process gas access pipeline, it imports described processed gas;
Pretreatment adsorption tank, it is arranged at described processing gas access pipeline, and holds pretreatment adsorbent,
Described recovering mechanism portion, has:
Reflux gas pipeline, it makes the reflux gas of being extruded from described condenser and/or separator by described desorption gas turn back to the upstream side of adsorption tank for the pretreatment of described processing gas access pipeline.
2. gas treatment equipment according to claim 1, wherein, described adsorbent is NACF or granular active carbon.
3. gas treatment equipment according to claim 1 and 2, is characterized in that, described pretreatment is at least one of granular active carbon, NACF, zeolite, silica gel, ion exchange resin and activated alumina group with adsorbent.
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| JP2013016770A JP6085977B2 (en) | 2013-01-31 | 2013-01-31 | Gas processing apparatus and gas processing method |
| JP2013-016770 | 2013-01-31 |
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| JP3183381B2 (en) * | 1995-09-06 | 2001-07-09 | 東邦化工建設株式会社 | Method for recovering organic solvent from small air volume gas containing high concentration organic solvent |
| JPH10323535A (en) * | 1997-05-27 | 1998-12-08 | Ishikawajima Harima Heavy Ind Co Ltd | Waste gas deodorizing method and waste gas deodorizing device |
| JP2001179041A (en) * | 1999-12-27 | 2001-07-03 | Toyobo Co Ltd | Gas treatment equipment |
| JP2001347126A (en) * | 2000-06-09 | 2001-12-18 | Toyobo Co Ltd | Gas treating device and gas treating method |
| JP4596110B2 (en) * | 2001-07-19 | 2010-12-08 | 東洋紡績株式会社 | Gas processing apparatus and gas processing method |
| JP4305719B2 (en) * | 2002-09-13 | 2009-07-29 | 東洋紡績株式会社 | Organic solvent processing equipment |
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2013
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| JP2014147863A (en) | 2014-08-21 |
| JP6085977B2 (en) | 2017-03-01 |
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