CN107879313A - A kind of processing method and system of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid - Google Patents
A kind of processing method and system of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid Download PDFInfo
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- CN107879313A CN107879313A CN201711167142.7A CN201711167142A CN107879313A CN 107879313 A CN107879313 A CN 107879313A CN 201711167142 A CN201711167142 A CN 201711167142A CN 107879313 A CN107879313 A CN 107879313A
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 title claims abstract description 127
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 239000006227 byproduct Substances 0.000 title claims abstract description 48
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000005660 chlorination reaction Methods 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 19
- 230000008569 process Effects 0.000 title claims abstract description 18
- 238000003672 processing method Methods 0.000 title claims abstract description 13
- 238000000605 extraction Methods 0.000 claims abstract description 95
- 239000007788 liquid Substances 0.000 claims abstract description 35
- 229920000049 Carbon (fiber) Polymers 0.000 claims abstract description 12
- 239000004917 carbon fiber Substances 0.000 claims abstract description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 7
- 238000005406 washing Methods 0.000 claims abstract description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N monobenzene Natural products C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 25
- 238000003795 desorption Methods 0.000 claims description 12
- 230000008676 import Effects 0.000 claims description 9
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims description 2
- 125000003944 tolyl group Chemical group 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 abstract description 10
- 238000004064 recycling Methods 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000005416 organic matter Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 4
- 229910052801 chlorine Inorganic materials 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- -1 extraction tower Chemical compound 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- ZPHQBFRCXUIIAZ-UHFFFAOYSA-N benzene;hydrochloride Chemical compound Cl.C1=CC=CC=C1 ZPHQBFRCXUIIAZ-UHFFFAOYSA-N 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0731—Purification ; Separation of hydrogen chloride by extraction
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0718—Purification ; Separation of hydrogen chloride by adsorption
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses the processing method and system of a kind of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid, the by-product hydrochloric acid that toluene or chlorotoluene chlorination system come out enters at the top of extraction tower, extractant enters from extraction tower bottom, the counter current contacting in extraction tower, extractant absorbs the organic matter in by-product hydrochloric acid, from extraction tower overhead extraction, raffinate phase produces the bottom for being sent into PAN-ACF tower from tower reactor, extractant in PAN-ACF raffinate phase, tail washings hydrochloric acid sterling after absorption reaches technical grade, discharged by PAN-ACF column overhead, into storage tank；After carbon fiber penetrates, PAN-ACF tower is desorbed with vapor, the high-temperature vapor containing extractant condenses into condenser, and condensate liquid enters extraction tank and carries out water-oil separating, and the oil phase of recovery is back in extraction tower.By-product hydrochloric acid has reached the quality requirement of technical grade, economized on resources, realized recycling economy development and environmental protection after processing.
Description
Technical field
The present invention relates to the recycling process field of accessory substance in chemical process, more particularly to a kind of toluene or chlorine
The processing method and system of by-product hydrochloric acid in chlorination toluene production process.
Background technology
It can be produced in chlorine chemical industry especially toluene and the production process of chlorotoluene chlorination substantial amounts of side product chlorinated
Hydrogen (HC1), these chlorine water multi-purpose greatly absorb by-product hydrochloric acid, because wherein containing a certain amount of organic impurities, toluene and chlorotoluene, reached
Less than industrial requirements, its purposes is restricted greatly, and some areas are directly discharged after even being neutralized with alkali, not only influences chlorine products production
Economic benefit, and cause the wasting of resources, pollute environment, this mode is unsustainable.
The content of the invention
The invention provides the processing method of a kind of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid, by-product hydrochloric acid
After treatment by using the treatment method, reach the quality requirement of technical grade, economized on resources, realize recycling economy development and environmental protection.
In order to solve the above problems, the technical solution adopted in the present invention is a kind of such, chlorination toluene production process
The processing method of middle by-product hydrochloric acid, comprises the following steps：
1）The by-product hydrochloric acid that chlorination toluene system comes out enters at the top of extraction tower, and extractant enters from extraction tower bottom, is extracting
Take counter current contacting in tower, extractant absorbs the toluene and chlorotoluene in by-product hydrochloric acid, and from extraction tower overhead extraction, raffinate phase is from tower
Kettle produces；Wherein, described extractant is benzene；
2）The raffinate phase of tower reactor extraction is sent into the bottom of PAN-ACF tower, the extractant in PAN-ACF raffinate phase, inhaled
Attached tail washings hydrochloric acid sterling reaches technical grade, is discharged by PAN-ACF column overhead, into storage tank.
3）After carbon fiber penetrates, PAN-ACF tower is desorbed with vapor, the high-temperature water containing extractant steams
Gas condenses into condenser, and condensate liquid enters extraction tank and carries out water-oil separating, and the oil phase of recovery, which is back to circulation in extraction tower, to be made
With.
Recycled to realize, when the toluene in extractant absorption by-product hydrochloric acid and chlorotoluene total concentration reach 31%-33
% V/V, from extraction tower overhead extraction, rectifying column is discharged into, the extractant for removing gained after toluene and chlorotoluene returns again to extraction tower
Interior recycling.
A kind of processing method of chlorotoluene chlorination production byproduct in process hydrochloric acid, it is characterised in that comprise the following steps：
1）The by-product hydrochloric acid that chlorotoluene chlorination system comes out enters at the top of extraction tower, and extractant enters from extraction tower bottom,
Counter current contacting in extraction tower, extractant absorbs the chlorotoluene and dichlorotoleune in by-product hydrochloric acid, from extraction tower overhead extraction, raffinate
Mutually produced from tower reactor；Wherein, described extractant is toluene；
2）The raffinate phase of tower reactor extraction is sent into the bottom of PAN-ACF tower, the extractant in PAN-ACF raffinate phase, inhaled
Attached tail washings hydrochloric acid sterling reaches technical grade, is discharged by PAN-ACF column overhead, into storage tank；
3）After carbon fiber penetrates, PAN-ACF tower is desorbed with vapor, the high-temperature vapor containing extractant enters
Enter condenser condensation, condensate liquid enters extraction tank and carries out water-oil separating, and the oil phase of recovery, which is back in extraction tower, to be recycled.
Recycled to realize, when the chlorotoluene in extractant absorption by-product hydrochloric acid and dichlorotoleune total concentration reach
31%-33 % V/V, from extraction tower overhead extraction, rectifying column is discharged into, removes the extractant of gained after chlorotoluene and dichlorotoleune again
Return in extraction tower and recycle.
Handling toluene or during chlorotoluene chlorination production byproduct in process hydrochloric acid, during extraction, temperature is 30-- in extraction tower
80 DEG C, 0.1-0.2Mpa of pressure；During absorption, temperature is 30--80 DEG C in carbon fiber absorption tower, and pressure is 0.05-0.1Mpa；
During desorption, it is 100--180 DEG C that carbon fiber, which absorbs tower temperature degree, and pressure is 0.1-0.2Mpa；
The present invention also provides a kind of processing system of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid, including extraction tower,
PAN-ACF tower, storage tank, steam raising plant, condenser and extraction tank, the heavy liquid exit and carbon of described extraction tower
The inlet of fibers adsorption tower bottom is connected, and the liquid outlet of PAN-ACF top of tower is connected with storage tank；Described steam hair
Generating apparatus is connected by steam inlet tube with the desorption gas entrance of PAN-ACF tower, and the desorption gas of PAN-ACF tower bottom goes out
Mouth is connected with the air inlet import of condenser, and the condensate outlet of condenser is connected with extraction tank entrance, the oil phase of extraction tank
Outlet is incorporated to the extractant inlet pipe being connected with the heavy liquid inlet of extraction tower.
Preferably, the top of described PAN-ACF tower is horizontal discharge case, and the discharge case one end passes through absorbing carbon fiber
The side wall of attached tower is stretched into PAN-ACF tower, and the bottom that discharge case is located at the outer one end of PAN-ACF tower is provided with delivery pipe,
Afflux groove is provided with below the delivery pipe, the afflux groove is connected with delivery pipe, and described liquid outlet is arranged under afflux groove
Portion.
Preferably, it is provided with primary filter screen in described discharge case.
It is further preferred that secondary filter is provided with described delivery pipe, the aperture ratio primary filter screen hole of secondary filter
Footpath is small.
Beneficial effect：
1st, after by-product hydrochloric acid is processed by the invention, the quality requirement of technical grade has been reached.
2nd, the technology of the present invention significant effect, extractant cyclic absorption in extraction tower, the toluene carried secretly in by-product hydrochloric acid with
Chlorotoluene or chlorotoluene and dichlorotoleune organic matter, almost all are recovered processing and recycled, both saved resource and into
This, protects environment, technological operation simple possible, operating cost again.
3rd, carbon fiber can be used with desorption and regeneration, realize the recycling to extractant, reduce solid waste, recovered material,
Reduce consumption.
Brief description of the drawings
Fig. 1 is schematic structural view of the invention.
Fig. 2 is the structural representation of A in Fig. 1.
Embodiment
In order to deepen the understanding of the present invention, below in conjunction with embodiment and accompanying drawing, the invention will be further described, should
Embodiment is only used for explaining the present invention, is not intended to limit the scope of the present invention..
Embodiment 1
Referring to Fig. 1, a kind of processing system of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid, including extraction tower 1, carbon are fine
Tie up adsorption tower 2, storage tank 3, steam raising plant, condenser 4 and extraction tank 5, the heavy liquid exit and carbon fiber of described extraction tower 1
The inlet of the bottom of adsorption tower 2 is connected, and the liquid outlet at the top of PAN-ACF tower 2 is connected with storage tank 3；Described steam generation
Device（Not shown in Fig. 1）It is connected by steam inlet tube with the desorption gas entrance of PAN-ACF tower 2, the bottom of PAN-ACF tower 2
The desorption gas outlet in portion is connected with the air inlet import of condenser 4, and the condensate outlet of condenser 4 is connected with the entrance of extraction tank 5
Logical, the oil phase outlet of extraction tank 5 is incorporated to the extractant inlet pipe being connected with the heavy liquid inlet of extraction tower 1.
The light liquid outlet of described extraction tower is connected with the entrance of rectifying column 6, and the liquid outlet of the bottom of rectifying column 6 is incorporated to and extracted
The connected extractant inlet pipe in the heavy liquid inlet of tower 1.
The top of described PAN-ACF tower is horizontal discharge case 6, and the one end of discharge case 6 passes through PAN-ACF tower
Side wall is stretched into PAN-ACF tower, and the bottom that discharge case is located at the outer one end of PAN-ACF tower is provided with delivery pipe 7, the discharge
The lower section of pipe 7 is provided with afflux groove 8, and the afflux groove 8 is connected with delivery pipe 7, and described liquid outlet is arranged under afflux groove 8
Portion.
Primary filter screen 9 is provided with described discharge case, secondary filter 10, secondary filter are provided with described delivery pipe
10 aperture of aperture ratio primary filter screen 11 is small.
Embodiment 2
The processing method of by-product hydrochloric acid, comprises the following steps in a kind of chlorination toluene production process：
1）The by-product hydrochloric acid that chlorination toluene system comes out（Including 31-33W/W% of toluene, 31-33W/W% of chlorotoluene and
31-33W/W% of hydrochloric acid）Enter from the light liquid import at the top of extraction tower 1, the heavy-fluid import of extractant benzene from the bottom of extraction tower 1 is entered
Enter, the weight ratio of by-product hydrochloric acid and extractant is 8:5, the counter current contacting in extraction tower, it is 40 DEG C to control temperature in extraction tower, pressure
Power is 0.15Mpa, and extractant benzene absorbs the toluene and chlorotoluene in by-product hydrochloric acid, is produced from the light liquid import of extraction column overhead,
Raffinate phase produces from the heavy liquid exit of tower reactor；
2）The inlet that the raffinate phase of tower reactor extraction is sent into the bottom of PAN-ACF tower 2 enters PAN-ACF tower 2, raffinate phase
Charging liquid hourly space velocity (LHSV) is 2hr-1, adsorption temp is 40 DEG C, pressure 0.05Mpa, the extractant in PAN-ACF raffinate phase
Benzene, the tail washings hydrochloric acid sterling after absorption reaches technical grade, discharged by PAN-ACF column overhead, into storage tank 3.
3）After carbon fiber penetrates, PAN-ACF tower 2 is desorbed with vapor, water vapour charging liquid hourly space velocity (LHSV) is
2.5 hr-1, 100--180 DEG C of desorption temperature, pressure 0.15Mpa, after desorption, the high-temperature vapor containing benzene enters condensation
Device 4 condenses, and condensate liquid enters extraction tank 5 and carries out water-oil separating, the oil phase of recovery（Benzene）It is back in extraction tower 4 and recycles.
Recycled to realize, when the toluene in extractant benzene absorption by-product hydrochloric acid and chlorotoluene total concentration reach 31%-
33 % w/w, from extraction tower overhead extraction, rectifying column is discharged into, the extractant for removing gained after toluene and chlorotoluene returns again to extraction
Recycled in tower.
Embodiment 2
A kind of processing method of chlorotoluene chlorination production byproduct in process hydrochloric acid, comprises the following steps：
1）The light liquid import at the by-product hydrochloric acid that first chlorotoluene chlorination system comes out from the top of extraction tower 1 enters, extractant toluene from
The heavy-fluid import of the bottom of extraction tower 1 enters, and the weight ratio of by-product hydrochloric acid and extractant is 8:5, the counter current contacting in extraction tower, control
Temperature is 40 DEG C, pressure 0.15Mpa in extraction tower processed, and extractant toluene absorbs the chlorotoluene and dichloromethane in by-product hydrochloric acid
Benzene, from the light liquid import extraction of extraction column overhead, raffinate phase produces from the heavy liquid exit of tower reactor；
2）The inlet that the raffinate phase of tower reactor extraction is sent into the bottom of PAN-ACF tower 2 enters PAN-ACF tower 2, raffinate phase
Charging liquid hourly space velocity (LHSV) is 2hr-1, adsorption temp is 40 DEG C, pressure 0.05Mpa, the extractant in PAN-ACF raffinate phase
Toluene, the tail washings hydrochloric acid sterling after absorption reaches technical grade, discharged by PAN-ACF column overhead, into storage tank 3.
3）After carbon fiber penetrates, PAN-ACF tower 2 is desorbed with vapor, water vapour charging liquid hourly space velocity (LHSV) is
2.5 hr-1 , 100--180 DEG C of desorption temperature, pressure 0.15Mpa, after desorption, the high-temperature vapor containing toluene enters cold
Condenser 4 condenses, and condensate liquid enters extraction tank 5 and carries out water-oil separating, the oil phase of recovery（Toluene）Being back to circulation in extraction tower 4 makes
With.
Recycled to realize, when the chlorotoluene in extractant benzene absorption by-product hydrochloric acid and dichlorotoleune total concentration reach
31%-33 % w/w, from extraction tower overhead extraction, rectifying column is discharged into, removes the extractant of gained after chlorotoluene and dichlorotoleune again
Return in extraction tower and recycle.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
God any modification, equivalent substitution and improvements made etc., should be included in the scope of the protection with principle.
Claims (9)
1. the processing method of by-product hydrochloric acid in a kind of chlorination toluene production process, it is characterised in that comprise the following steps：
1）The by-product hydrochloric acid that chlorination toluene system comes out enters at the top of extraction tower, and extractant enters from extraction tower bottom, is extracting
Take counter current contacting in tower, extractant absorbs the toluene and chlorotoluene in by-product hydrochloric acid, and from extraction tower overhead extraction, raffinate phase is from tower
Kettle produces；Wherein, described extractant is benzene；
2）The raffinate phase of tower reactor extraction is sent into the bottom of PAN-ACF tower, the extractant in PAN-ACF raffinate phase, inhaled
Attached tail washings hydrochloric acid sterling reaches technical grade, is discharged by PAN-ACF column overhead, into storage tank；
3）After carbon fiber penetrates, PAN-ACF tower is desorbed with vapor, the high-temperature vapor containing extractant enters
Enter condenser condensation, condensate liquid enters extraction tank and carries out water-oil separating, and the oil phase of recovery, which is back in extraction tower, to be recycled.
2. the processing method of a kind of toluene according to claim 1 or chlorotoluene chlorination production byproduct in process hydrochloric acid, its
It is characterised by, is discharged to rectifying column from the extraction phase of extraction tower overhead extraction, removes the extractant of gained after toluene and chlorotoluene
Return again in extraction tower and circulate.
3. the processing method of a kind of toluene according to claim 1 or 2 or chlorotoluene chlorination production byproduct in process hydrochloric acid,
Characterized in that, when extractant absorb by-product hydrochloric acid in toluene and chlorotoluene total concentration reach 31%-33% W/W, from extraction tower
Overhead extraction.
4. a kind of processing method of chlorotoluene chlorination production byproduct in process hydrochloric acid, it is characterised in that comprise the following steps：
1）The by-product hydrochloric acid that chlorotoluene chlorination system comes out enters at the top of extraction tower, and extractant enters from extraction tower bottom,
Counter current contacting in extraction tower, extractant absorbs the chlorotoluene and dichlorotoleune in by-product hydrochloric acid, from extraction tower overhead extraction, raffinate
Mutually produced from tower reactor；Wherein, described extractant is toluene；
2）The raffinate phase of tower reactor extraction is sent into the bottom of PAN-ACF tower, the extractant in PAN-ACF raffinate phase, inhaled
Attached tail washings hydrochloric acid sterling reaches technical grade, is discharged by PAN-ACF column overhead, into storage tank；
3）After carbon fiber penetrates, PAN-ACF tower is desorbed with vapor, the high-temperature vapor containing extractant enters
Enter condenser condensation, condensate liquid enters extraction tank and carries out water-oil separating, and the oil phase of recovery, which is back in extraction tower, to be recycled.
A kind of 5. processing system of toluene or chlorotoluene chlorination production byproduct in process hydrochloric acid, it is characterised in that including extraction tower,
PAN-ACF tower, storage tank, steam raising plant, condenser and extraction tank, the heavy liquid exit and carbon of described extraction tower
The inlet of fibers adsorption tower bottom is connected, and the liquid outlet of PAN-ACF top of tower is connected with storage tank；Described steam hair
Generating apparatus is connected by steam inlet tube with the desorption gas entrance of PAN-ACF tower, and the desorption gas of PAN-ACF tower bottom goes out
Mouth is connected with the air inlet import of condenser, and the condensate outlet of condenser is connected with extraction tank entrance, the oil phase of extraction tank
Outlet is incorporated to the extractant inlet pipe being connected with the heavy liquid inlet of extraction tower.
6. the processing system of a kind of toluene according to claim 5 or chlorotoluene chlorination production byproduct in process hydrochloric acid, its
It is characterised by, the light liquid outlet of described extraction tower is connected with rectifying column inlet, and the liquid outlet of rectifier bottoms is incorporated to and extracted
The connected extractant inlet pipe in the heavy liquid inlet of tower.
7. the processing system of a kind of toluene according to claim 5 or chlorotoluene chlorination production byproduct in process hydrochloric acid, its
It is characterised by, the top of described PAN-ACF tower is horizontal discharge case, and the discharge case one end passes through PAN-ACF tower
Side wall is stretched into PAN-ACF tower, and the bottom that discharge case is located at the outer one end of PAN-ACF tower is provided with delivery pipe, the discharge
Afflux groove is provided with below pipe, the afflux groove is connected with delivery pipe, and described liquid outlet is arranged at the bottom of afflux groove.
8. the processing system of a kind of toluene according to claim 5 or chlorotoluene chlorination production byproduct in process hydrochloric acid, its
It is characterised by, primary filter screen is provided with described discharge case.
9. the processing system of a kind of toluene according to claim 5 or chlorotoluene chlorination production byproduct in process hydrochloric acid, its
It is characterised by, secondary filter is provided with described delivery pipe, and the aperture ratio primary filter screen aperture of secondary filter is small.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110255501A (en) * | 2019-07-11 | 2019-09-20 | 金宏气体电子材料（淮安）有限责任公司 | A kind of electronic grade high-purity hydrogen chloride preparation method |
| CN114291792A (en) * | 2022-02-07 | 2022-04-08 | 宁波环洋新材料股份有限公司 | Method for recycling hydrogen chloride from byproduct hydrochloric acid solution |
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| JPS646002A (en) * | 1987-06-30 | 1989-01-10 | Nippon Carbide Kogyo Kk | Post-treatment of post-chlorinated vinyl chloride polymer |
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|---|---|---|---|---|
| CN110255501A (en) * | 2019-07-11 | 2019-09-20 | 金宏气体电子材料（淮安）有限责任公司 | A kind of electronic grade high-purity hydrogen chloride preparation method |
| CN114291792A (en) * | 2022-02-07 | 2022-04-08 | 宁波环洋新材料股份有限公司 | Method for recycling hydrogen chloride from byproduct hydrochloric acid solution |
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