CN108083965A - A kind of recycling technique of toluene - Google Patents
A kind of recycling technique of toluene Download PDFInfo
- Publication number
- CN108083965A CN108083965A CN201711275362.1A CN201711275362A CN108083965A CN 108083965 A CN108083965 A CN 108083965A CN 201711275362 A CN201711275362 A CN 201711275362A CN 108083965 A CN108083965 A CN 108083965A
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- CN
- China
- Prior art keywords
- toluene
- evaporator
- tube side
- liquid
- adsorption tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 title claims abstract description 266
- 238000004064 recycling Methods 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000001179 sorption measurement Methods 0.000 claims abstract description 33
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 17
- 239000002912 waste gas Substances 0.000 claims abstract description 14
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 230000008020 evaporation Effects 0.000 claims abstract description 10
- 239000012141 concentrate Substances 0.000 claims abstract description 8
- QTWJRLJHJPIABL-UHFFFAOYSA-N 2-methylphenol;3-methylphenol;4-methylphenol Chemical compound CC1=CC=C(O)C=C1.CC1=CC=CC(O)=C1.CC1=CC=CC=C1O QTWJRLJHJPIABL-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 239000000428 dust Substances 0.000 claims abstract description 5
- 239000000835 fiber Substances 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000012432 intermediate storage Methods 0.000 claims description 8
- 238000013316 zoning Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 239000002250 absorbent Substances 0.000 claims description 4
- 230000002745 absorbent Effects 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 238000003795 desorption Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 238000010792 warming Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 8
- 238000000926 separation method Methods 0.000 abstract description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 230000008901 benefit Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000003444 anaesthetic effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 description 1
- 229940073608 benzyl chloride Drugs 0.000 description 1
- 125000001797 benzyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])* 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 210000003169 central nervous system Anatomy 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 230000003907 kidney function Effects 0.000 description 1
- 230000003908 liver function Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 210000004400 mucous membrane Anatomy 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 230000000638 stimulation Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of recycling technique of toluene, the recycling technique of the toluene is as follows：S1：Order needs the crude cresylic acid recycled into the tube side of the first evaporator, crude cresylic acid in the tube side of first evaporator is heated, toluene liquid after the first evaporator is tentatively concentrated by evaporation is transported to by concentrate pump in the tube side of the second evaporator, simultaneously, the toluene vapor that the tube side of the first evaporator comes out is made to enter the shell side of the second evaporator, the toluene liquid of initial concentration carries out heating evaporation in the second evaporator tube side；S2：Toluene waste gas in the second evaporator is expelled to filter via through pipeline using the first exhaust fan, the fiber in exhaust gas and dust are separated；The present invention is desorbed by activated carbon adsorption, steam, condenser condenses, the respective recycling after aqueous vapor separation is utilizing, and recovery utilization rate is high.
Description
Technical field
The present invention relates to the recycling techniques of the utilization technology field of toluene, specially a kind of toluene.
Background technology
Toluene is a kind of industrial chemicals, and benzyl compounds conduction oil can be synthesized with benzyl chloride.But the mother after conduction oil synthesis
Liquid requires toluene to evaporate as early as possible totally in subsequent handling.Toluene has low boiling point (110.6 DEG C of boiling point), volatile etc. in itself
Feature, and toluene is a kind of substance for having certain toxicity, and steam has stimulation to human skin, mucous membrane, while right
Central nervous system has anesthetic effect, and long term can influence hepatic and renal function.Therefore, the highest permission of toluene is dense in workshop air
It spends for 40mg/m3.Toluene is a kind of very common solvent, and because its flash-point is low, volatile, dirt can be caused to air after discharge
Dye, it is therefore desirable to be recycled.And traditional recovery technology can only accomplish economic benefits and social benefits, heat utilization ratio is low, of high cost, does not meet mesh
The requirement of preceding international and domestic industry energy-saving and emission-reduction there is an urgent need to reduce recycling energy consumption, reduces production cost in view of above-mentioned toluene
Physicochemical characteristic, it is domestic to be equipped with purifier in the place for much generating exhaust gas.
The content of the invention
It is mentioned above in the background art to solve it is an object of the invention to provide a kind of recycling technique of toluene
Problem.
To achieve the above object, the present invention provides following technical solution：A kind of recycling technique of toluene, the toluene
Technique is recycled to be as follows：
S1：Order needs the crude cresylic acid recycled into the tube side of the first evaporator, to the thick first in the tube side of the first evaporator
Benzene is heated, and the toluene liquid after the first evaporator is tentatively concentrated by evaporation is transported to the second evaporator by concentrate pump
In tube side, meanwhile, the toluene vapor that the tube side of the first evaporator comes out is made to enter the shell side of the second evaporator, the second evaporator tube
The toluene liquid of initial concentration carries out heating evaporation in journey；
S2：Toluene waste gas in the second evaporator is expelled to filter via through pipeline using the first exhaust fan, by exhaust gas
In fiber and dust separated；
S3：It is extracted by the toluene waste gas of filter by vacuum system after the condensation of vertical array tubular condenser, toluene gives up
Gas enters adsorption tower by admission line, and it is inverse that gas-liquid is carried out under 30-50 DEG C, 0.5~1.0MPa with the absorbent that tower top sprays into
Stream contact, when toluene waste gas absorptivity reaches 90-95%, above-mentioned toluene solution is sent to desorber, 90-100 DEG C, 0.1
It is desorbed under~0.13MPa, exhaust gas is adsorbed via activated carbon adsorption baffle in adsorption tower, the gas without toluene after absorption
It is discharged from adsorption tower exhaust outlet；
S4：When activated carbon adsorption baffle adsorbs toluene to saturation, the intake valve, air outlet valve and row of adsorption tower are simultaneously closed off
Empty valve opens the water vapour valve of adsorption tower, and the steam for being passed through 0.5~0.8MPa is heated, it is allowed to be warming up to 110~115
℃；
S5：Toluene, hot water and water vapour through desorption enter cooler, are cooled to room temperature, when cooling time is 3-5 small,
After mixing liquid after cooling enters AUTOMATIC ZONING device AUTOMATIC ZONING, upper toluene flows into toluene intermediate storage tank by upper outlet,
Lower floor's clear water discharge, the toluene of intermediate storage tank are pumped to methylbenzene raw material slot.
Preferably, the first evaporator controls going out for concentrate pump by high viscosity pressure difference liquid level sensor in the step S1
Expect speed.
Preferably, the first evaporator and the second evaporator control steam pneumatic operated valve by temperature sensor in the step S1
Aperture, to control the inlet of steam, so as to control the balance entirely evaporated.
Compared with prior art, the beneficial effects of the invention are as follows：The present invention is desorbed by activated carbon adsorption, steam, condensation
Device condenses, the respective recycling after aqueous vapor separation is utilizing, and recovery utilization rate is high, and simple in structure, advantages of good adsorption effect, repetition profit
With rate is high, service life is long, cost recovery is low, operating cost can be reduced, purifies air, energy-saving and emission-reduction, similary area is set
Standby, recovery processing ability greatly improves, and multistage recycling, toluene purity is high, stable quality.
Specific embodiment
In order to make the purpose , technical scheme and advantage of the present invention be clearer, below in conjunction with specific embodiment, to this
Invention is further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, not
For limiting the present invention.
Embodiment 1
A kind of recycling technique of toluene, the recycling technique of the toluene are as follows：
S1：Order needs the crude cresylic acid recycled into the tube side of the first evaporator, to the thick first in the tube side of the first evaporator
Benzene is heated, and the toluene liquid after the first evaporator is tentatively concentrated by evaporation is transported to the second evaporator by concentrate pump
In tube side, meanwhile, the toluene vapor that the tube side of the first evaporator comes out is made to enter the shell side of the second evaporator, the second evaporator tube
The toluene liquid of initial concentration carries out heating evaporation in journey；
S2：Toluene waste gas in the second evaporator is expelled to filter via through pipeline using the first exhaust fan, by exhaust gas
In fiber and dust separated；
S3：It is extracted by the toluene waste gas of filter by vacuum system after the condensation of vertical array tubular condenser, toluene gives up
Gas enters adsorption tower by admission line, and gas-liquid counter current is carried out under 50 DEG C, 1.0MPa with the absorbent that tower top sprays into contacts, when
When toluene waste gas absorptivity reaches 90-95%, above-mentioned toluene solution is sent to desorber, is solved under 100 DEG C, 0.13MPa
It inhales, exhaust gas is adsorbed via activated carbon adsorption baffle in adsorption tower, and the gas without toluene after absorption is arranged from adsorption tower exhaust outlet
Go out；
S4：When activated carbon adsorption baffle adsorbs toluene to saturation, the intake valve, air outlet valve and row of adsorption tower are simultaneously closed off
Empty valve opens the water vapour valve of adsorption tower, and the steam for being passed through 0.8MPa is heated, it is allowed to be warming up to 110 DEG C；
S5：Toluene, hot water and water vapour through desorption enter cooler, are cooled to room temperature, cold when cooling time is 3 small
But after the mixing liquid after enters AUTOMATIC ZONING device AUTOMATIC ZONING, upper toluene flows into toluene intermediate storage tank by upper outlet, under
Layer clear water discharge, the toluene of intermediate storage tank are pumped to methylbenzene raw material slot.
The first evaporator controls the discharging speed of concentrate pump by high viscosity pressure difference liquid level sensor in the step S1.
The first evaporator and the second evaporator control the aperture of steam pneumatic operated valve by temperature sensor in the step S1,
The inlet of steam is controlled, so as to controlling the balance entirely evaporated.
Embodiment 2
A kind of recycling technique of toluene, the recycling technique of the toluene are as follows：
S1：Order needs the crude cresylic acid recycled into the tube side of the first evaporator, to the thick first in the tube side of the first evaporator
Benzene is heated, and the toluene liquid after the first evaporator is tentatively concentrated by evaporation is transported to the second evaporator by concentrate pump
In tube side, meanwhile, the toluene vapor that the tube side of the first evaporator comes out is made to enter the shell side of the second evaporator, the second evaporator tube
The toluene liquid of initial concentration carries out heating evaporation in journey；
S2：Toluene waste gas in the second evaporator is expelled to filter via through pipeline using the first exhaust fan, by exhaust gas
In fiber and dust separated；
S3：It is extracted by the toluene waste gas of filter by vacuum system after the condensation of vertical array tubular condenser, toluene gives up
Gas enters adsorption tower by admission line, and gas-liquid counter current is carried out under 30 DEG C, 0.5MPa with the absorbent that tower top sprays into contacts, when
When toluene waste gas absorptivity reaches 90-95%, above-mentioned toluene solution is sent to desorber, is desorbed under 90 DEG C, 0.1MPa,
Exhaust gas is adsorbed via activated carbon adsorption baffle in adsorption tower, and the gas without toluene after absorption is discharged from adsorption tower exhaust outlet；
S4：When activated carbon adsorption baffle adsorbs toluene to saturation, the intake valve, air outlet valve and row of adsorption tower are simultaneously closed off
Empty valve opens the water vapour valve of adsorption tower, and the steam for being passed through 0.5MPa is heated, it is allowed to be warming up to 115 DEG C；
S5：Toluene, hot water and water vapour through desorption enter cooler, are cooled to room temperature, when cooling time is 3-5 small,
After mixing liquid after cooling enters AUTOMATIC ZONING device AUTOMATIC ZONING, upper toluene flows into toluene intermediate storage tank by upper outlet,
Lower floor's clear water discharge, the toluene of intermediate storage tank are pumped to methylbenzene raw material slot.
The present invention is desorbed by activated carbon adsorption, steam, condenser condenses, the respective recycling after aqueous vapor separation is utilizing,
Its recovery utilization rate is high, and simple in structure, advantages of good adsorption effect, high recycling rate, service life are long, cost recovery is low, can
Operating cost is reduced, purifies air, energy-saving and emission-reduction, the equipment of similary area, recovery processing ability greatly improves, multistage to recycle,
Toluene purity is high, stable quality.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto,
Any one skilled in the art in the technical scope disclosed by the present invention, technique according to the invention scheme and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (3)
1. a kind of recycling technique of toluene, it is characterised in that：The recycling technique of the toluene is as follows：
S1：Order needs the crude cresylic acid that recycles to enter the tube side of the first evaporator, to the crude cresylic acid in the tube side of the first evaporator into
Row heating, the toluene liquid after the first evaporator is tentatively concentrated by evaporation are transported to the tube side of the second evaporator by concentrate pump
In, meanwhile, the toluene vapor that the tube side of the first evaporator comes out is made to enter the shell side of the second evaporator, in the second evaporator tube side
The toluene liquid of initial concentration carries out heating evaporation；
S2：Toluene waste gas in the second evaporator is expelled to filter via through pipeline using the first exhaust fan, it will be in exhaust gas
Fiber and dust are separated；
S3：It is extracted by the toluene waste gas of filter by vacuum system after the condensation of vertical array tubular condenser, toluene waste gas leads to
It crosses admission line and enters adsorption tower, the absorbent sprayed into tower top carries out gas-liquid counter current under 30-50 DEG C, 0.5~1.0MPa and connects
Touch, when toluene waste gas absorptivity reaches 90-95%, above-mentioned toluene solution is sent to desorber, 90-100 DEG C, 0.1~
Desorbed under 0.13MPa, exhaust gas is adsorbed via activated carbon adsorption baffle in adsorption tower, the gas without toluene after absorption from
Adsorption tower exhaust outlet is discharged；
S4：When activated carbon adsorption baffle adsorbs toluene to saturation, the intake valve, air outlet valve and emptying of adsorption tower are simultaneously closed off
Valve opens the water vapour valve of adsorption tower, and the steam for being passed through 0.5~0.8MPa is heated, it is allowed to be warming up to 110~115 DEG C；
S5：Toluene, hot water and water vapour through desorption enter cooler, are cooled to room temperature, when cooling time is 3-5 small, cooling
After mixing liquid afterwards enters AUTOMATIC ZONING device AUTOMATIC ZONING, upper toluene flows into toluene intermediate storage tank, lower floor by upper outlet
Clear water discharges, and the toluene of intermediate storage tank is pumped to methylbenzene raw material slot.
2. a kind of recycling technique of toluene according to claim 1, it is characterised in that：First steams in the step S1
Send out the discharging speed that device controls concentrate pump by high viscosity pressure difference liquid level sensor.
3. a kind of recycling technique of toluene according to claim 1, it is characterised in that：First steams in the step S1
The aperture that device and the second evaporator control steam pneumatic operated valve by temperature sensor is sent out, to control the inlet of steam, so as to control
Make the balance entirely evaporated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711275362.1A CN108083965A (en) | 2017-12-06 | 2017-12-06 | A kind of recycling technique of toluene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711275362.1A CN108083965A (en) | 2017-12-06 | 2017-12-06 | A kind of recycling technique of toluene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108083965A true CN108083965A (en) | 2018-05-29 |
Family
ID=62174445
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711275362.1A Pending CN108083965A (en) | 2017-12-06 | 2017-12-06 | A kind of recycling technique of toluene |
Country Status (1)
| Country | Link |
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Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1506099A (en) * | 1975-10-28 | 1978-04-05 | Inst Francais Du Petrole | Separation of hydrocarbons from mixtures |
| CN1597051A (en) * | 2003-09-15 | 2005-03-23 | 傅太平 | Method for recovering toluene from exhausted air |
| CN101229471A (en) * | 2007-11-09 | 2008-07-30 | 河北瑞通美邦工程有限公司 | Toluol-benzene solvent recovery technology from vent gas |
| CN102476012A (en) * | 2010-11-23 | 2012-05-30 | 大连创达技术交易市场有限公司 | Process for recycling and utilizing toluene |
| CN103223287A (en) * | 2013-04-27 | 2013-07-31 | 山东新华制药股份有限公司 | Purifying and recovering device of exhaust gas comprising toluene, and exhaust gas purifying and recovering method |
| JP2013163156A (en) * | 2012-02-10 | 2013-08-22 | Jfe Engineering Corp | Apparatus and method for treating exhaust gas containing volatile organic compound |
| US20130245351A1 (en) * | 2012-03-16 | 2013-09-19 | Saudi Arabian Oil Company | Recovery method and system for delivering extracted btx from gas streams |
| CN203634842U (en) * | 2013-10-16 | 2014-06-11 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple-effect toluene recycling device |
| CN104258687A (en) * | 2014-09-15 | 2015-01-07 | 常熟市振宇胶带有限公司 | Methylbenzene recovering device |
| CN104557421A (en) * | 2013-10-16 | 2015-04-29 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple-effect toluene recovery technology |
| CN105601461A (en) * | 2015-12-16 | 2016-05-25 | 安徽泰格生物技术股份有限公司 | Waste toluene recovery method in chemical production |
| CN205700025U (en) * | 2016-05-05 | 2016-11-23 | 江阴市友佳珠光云母有限公司 | A kind of mica tape production line methylbenzene recycling system |
-
2017
- 2017-12-06 CN CN201711275362.1A patent/CN108083965A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1506099A (en) * | 1975-10-28 | 1978-04-05 | Inst Francais Du Petrole | Separation of hydrocarbons from mixtures |
| CN1597051A (en) * | 2003-09-15 | 2005-03-23 | 傅太平 | Method for recovering toluene from exhausted air |
| CN101229471A (en) * | 2007-11-09 | 2008-07-30 | 河北瑞通美邦工程有限公司 | Toluol-benzene solvent recovery technology from vent gas |
| CN102476012A (en) * | 2010-11-23 | 2012-05-30 | 大连创达技术交易市场有限公司 | Process for recycling and utilizing toluene |
| JP2013163156A (en) * | 2012-02-10 | 2013-08-22 | Jfe Engineering Corp | Apparatus and method for treating exhaust gas containing volatile organic compound |
| US20130245351A1 (en) * | 2012-03-16 | 2013-09-19 | Saudi Arabian Oil Company | Recovery method and system for delivering extracted btx from gas streams |
| CN103223287A (en) * | 2013-04-27 | 2013-07-31 | 山东新华制药股份有限公司 | Purifying and recovering device of exhaust gas comprising toluene, and exhaust gas purifying and recovering method |
| CN203634842U (en) * | 2013-10-16 | 2014-06-11 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple-effect toluene recycling device |
| CN104557421A (en) * | 2013-10-16 | 2015-04-29 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple-effect toluene recovery technology |
| CN104258687A (en) * | 2014-09-15 | 2015-01-07 | 常熟市振宇胶带有限公司 | Methylbenzene recovering device |
| CN105601461A (en) * | 2015-12-16 | 2016-05-25 | 安徽泰格生物技术股份有限公司 | Waste toluene recovery method in chemical production |
| CN205700025U (en) * | 2016-05-05 | 2016-11-23 | 江阴市友佳珠光云母有限公司 | A kind of mica tape production line methylbenzene recycling system |
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| PB01 | Publication | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20180801 Address after: 201800 A4032 2, 2889 Baoan Road, Jiading District, Shanghai. Applicant after: Shanghai Jiu Xing conduction oil limited company Address before: 226200 No. 8, Binjiang Fine Chemical Industrial Park, Qidong, Nantong, Jiangsu. Applicant before: Qidong Long Star Chemical Co., Ltd. Applicant before: Shanghai Jiu Xing conduction oil limited company |
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| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20180529 |
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