CN203620613U - Heavy aromatics hydrogenation dealkylation lightweight reaction device - Google Patents
Heavy aromatics hydrogenation dealkylation lightweight reaction device Download PDFInfo
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- CN203620613U CN203620613U CN201320735440.2U CN201320735440U CN203620613U CN 203620613 U CN203620613 U CN 203620613U CN 201320735440 U CN201320735440 U CN 201320735440U CN 203620613 U CN203620613 U CN 203620613U
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- 238000006243 chemical reaction Methods 0.000 title claims description 19
- 238000005984 hydrogenation reaction Methods 0.000 title claims description 8
- 238000006900 dealkylation reaction Methods 0.000 title description 7
- 230000020335 dealkylation Effects 0.000 title 1
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 239000006200 vaporizer Substances 0.000 claims abstract description 12
- 239000007791 liquid phase Substances 0.000 claims abstract description 10
- 238000004458 analytical method Methods 0.000 claims abstract description 9
- 238000004817 gas chromatography Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 15
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 10
- 239000007792 gaseous phase Substances 0.000 claims description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 abstract description 18
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 abstract description 15
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 abstract description 12
- 239000008096 xylene Substances 0.000 abstract description 6
- 239000003054 catalyst Substances 0.000 description 9
- 239000000047 product Substances 0.000 description 5
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 125000000217 alkyl group Chemical group 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000001833 catalytic reforming Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 229910005855 NiOx Inorganic materials 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 229910052746 lanthanum Inorganic materials 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 229910052702 rhenium Inorganic materials 0.000 description 1
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
- 229910003158 γ-Al2O3 Inorganic materials 0.000 description 1
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Abstract
The utility model relates to a heavy aromatics hydrodealkylation and light conversion reaction device; the raw material H2 storage tank is connected with the mixer sequentially through a pressure reducing valve, a stop valve A, a filter A, a mass flow meter, a one-way valve A and a tee joint; raw material N2The storage tank is connected with the mixer sequentially through a stop valve B, a one-way valve B and a tee joint; the liquid raw material storage tank is connected with the mixer sequentially through the high-pressure liquid-phase micro metering pump and the one-way valve C; the mixer is connected with the vaporizer, and the vaporizer is connected with the reactor; the reactor is connected with a cooler tube side, and the cooler tube side is connected with a gas-liquid separator; a liquid phase outlet at the bottom of the gas-liquid separator is sequentially connected with an adjusting valve A, a sampler and an adjusting valve B; a gas outlet at the top of the gas-liquid separator is sequentially connected with a filter B, a back pressure valve, a six-way valve and a wet flowmeter, and the six-way valve is connected with a gas chromatography online analysis system; the device is suitable for preparing benzene, toluene and xylene by light aromatics, and the content of the xylene is high.
Description
Technical field
The utility model relates to a kind of heavy aromatics hydro-dealkylation lighting reaction unit.
Background technology
Heavy aromatics refers to the aromatic hydrocarbons of by-product in oil and coal process, is mainly C
9and C
10above aromatic hydrocarbons, it is mainly derived from oil plant catalytic reforming unit, polyester raw material factory long distillate catalytic reforming unit, ethylene unit, Lubricating oil refining device and coal high-temperature coking by-product heavy aromatics.Heavy aromatics complicated component, has up to a hundred components, is difficult to separate completely.Along with the increase of refining capacity, heavy aromatics output will increase substantially.
For a long time domestic to heavy aromatics utilize dynamics inadequate, except as partial solvent, major part is used as fuel burns, and not only wastes valuable resource, and causes environmental pollution.In the face of continuous perfect environmental law Laws & Regulations and domestic petroleum shortage of resources, effectively fully utilize Heavy Aromatic Hydrocarbons and produce the chemical products that various value is higher and just seem very necessary.
C at present
9it is carrier that+heavy aromatics hydro-dealkylation BTX processed mainly adopts oxide or molecular sieve, and carrying transition metal oxide or its metal are the catalyst of active component gained.Because the catalyst take molecular sieve as carrier gained is compared as the catalyst of carrier compared with oxide, there is low, the good acidity energy of reaction temperature, metal-modified catalytic performance and effectively suppress the advantages such as catalysqt deactivation, become C in recent years
9 +the main direction of heavy aromatics hydrodealkylation catalyst research.
CN1117404A invention a kind of in 30～70wt%(take carrier as benchmark) ZSM-5 zeolite and γ-Al2O3 or the η-Al2O3 of 30-70wt% be carrier, the platinum of the rhenium of load 0.1～0.5wt%, the tin of 0.1～0.5wt%, 0.05～0.3wt% or 0.2～0.8wt% composition.At 350～450 ℃, 0.5～3.5MPa, weight space velocity 1～5h
-1under the operating condition of hydrogen-hydrocarbon ratio (volume ratio) 500～1200, use this catalyst can improve C
9 +the productive rate of aromatics conversion rate and benzene and dimethylbenzene, C
9 +aromatics conversion rate and the growing amount of BTX reach respectively 27.0wt% and 25.2wt%.
CN101607207A invention is a kind of using H type MCM-56 and alchlor as composite carrier load IV A, V A, VII B, VIII family part metals element or its oxide are as active component, and this catalyst is applicable to the de-alkyl lighting reaction of heavy arene hydrogenation, C
9 +conversion ratio be 76.89%, BTX yield be 48.37%, BTX be selectively 80.50%, but the selective and stability of catalyst also needs further raising.
Utility model content
The de-alkyl lighting reaction unit of a kind of heavy arene hydrogenation the object of this invention is to provide.This device is applicable to heavy aromatics lighting and produces benzene, toluene and dimethylbenzene.Take NiOx as main active component and the metal oxide of Mo, Co, La or Cr be MCM-56 and the γ-Al of auxiliary activity component modification
2o
3for composite carried catalyst is to C
9 +the de-alkyl lighting reaction of heavy arene hydrogenation has catalyst action.C
9 +the conversion ratio of heavy aromatics is that the yield of 75.2%, BTX be 63.2%, BTX is selectively 84.2%, and in product, does not have ethylbenzene to generate.Xylene content is high, has improved heavy aromatics hydro-dealkylation and produce the selective and stability of benzene,toluene,xylene (BTX).
Heavy arene hydrogenation described in the utility model takes off alkyl lighting reaction unit, comprising: reactor, blender, vaporizer, cooler, gas-liquid separator, two gas circuits, liquid charging stock liquid road, on-line analysis system;
Raw material H in two gas circuits
2gas circuit, raw material H
2storage tank is connected with blender by pressure-reducing valve, stop valve A, filter A, mass flowmenter, check valve A, threeway successively; Another N
2gas circuit, raw material N
2storage tank is connected with blender by stop valve B, check valve B, threeway successively; The raw material storage tank on liquid charging stock liquid road is connected with blender by high pressure liquid phase Micro-metering Pumps, check valve C successively; Blender is connected with vaporizer, and vaporizer is connected with reactor; Reactor is connected with cooler tube side, and cooler tube side is connected with gas-liquid separator; The outlet of gas-liquid separator bottom liquid phases is connected with control valve A, sampler, control valve B in turn; Gas-liquid separator top gaseous phase outlet is connected with filter B, counterbalance valve, six-way valve and wet flow indicator in turn, and six-way valve is connected with gas-chromatography on-line analysis system simultaneously.
A N
2gas circuit is led to N
2, be mainly that reaction system is purged with deaeration; Another gas circuit is led to unstripped gas H
2, its flow is undertaken accurately controlling and metering by mass flowmenter, and liquid charging stock heavy aromatics imports reaction system, H by high pressure liquid phase Micro-metering Pumps
2first mix by threeway B with heavy aromatics, thereby then enter vaporizer heavy aromatics vaporization fully mixed; The product of outflow reactor, through cooler condensation, then enters vapour liquid separator; Liquid product that condensation is got off can sample after flowing into sampler, the emptying or enter gas-chromatography its composition is carried out to on-line analysis after counterbalance valve and wet flow indicator of not solidifying gas-phase product.
The de-alkyl lighting reaction unit of a kind of heavy arene hydrogenation described in the utility model is applicable to heavy aromatics lighting and produces benzene, toluene and dimethylbenzene.C
9 +the conversion ratio of heavy aromatics is that the yield of 75.2%, BTX be 63.2%, BTX is selectively 84.2%, and in product, does not have ethylbenzene to generate.Xylene content is high, has improved heavy aromatics hydro-dealkylation and produce the selective and stability of benzene,toluene,xylene (BTX).
Accompanying drawing explanation
Fig. 1 heavy aromatics hydro-dealkylation lighting reaction unit.
Wherein: 1 pressure-reducing valve, 2 stop valve A, 3 filter A, 4 mass flowmenters, 5 check valve A, 6 threeways, 7 stop valve B, 8 check valve B, 9 blenders, 10 high pressure liquid phase Micro-metering Pumps, 11 check valve C, 12 vaporizers, 13 reactors, 14 coolers, 15 gas-liquid separators, 16 control valve A, 17 samplers, 18 control valve B, 19 filter B, 20 counterbalance valves, 21 wet flow indicators, 22 six-way valves, 23 gas-chromatography on-line analysis systems.
The specific embodiment
Heavy arene hydrogenation described in the utility model takes off alkyl lighting reaction unit, comprising: reactor, blender, vaporizer, cooler, gas-liquid separator, two gas circuits, liquid charging stock liquid road, on-line analysis system;
Raw material H in two gas circuits
2gas circuit, raw material H
2storage tank is connected with blender 9 by pressure-reducing valve 1, stop valve A2, filter A3, mass flowmenter 4, check valve A5, threeway 6 successively; Another N
2gas circuit, raw material N
2storage tank is connected with blender 9 by stop valve B7, check valve B8, threeway 6 successively; The raw material storage tank on liquid charging stock liquid road is connected with blender 9 by high pressure liquid phase Micro-metering Pumps 10, check valve C11 successively; Blender 9 is connected with vaporizer 12, and vaporizer is connected with reactor 13; Reactor is connected with cooler 14 tube sides, and cooler tube side is connected with gas-liquid separator 15; The outlet of gas-liquid separator bottom liquid phases is connected with control valve A16, sampler 17, control valve B18 in turn; Gas-liquid separator top gaseous phase outlet is connected with filter B 19, counterbalance valve 20, six-way valve 22 and wet flow indicator 21 in turn, and six-way valve 22 is connected with gas-chromatography on-line analysis system 23 simultaneously.
Claims (1)
1. the de-alkyl lighting reaction unit of heavy arene hydrogenation, comprising: reactor, blender, vaporizer, cooler, gas-liquid separator, two gas circuits, liquid charging stock liquid road, on-line analysis system; It is characterized in that:
Raw material H in two gas circuits
2gas circuit, raw material H
2storage tank is connected with blender by pressure-reducing valve, stop valve A, filter A, mass flowmenter, check valve A, threeway successively; Another N
2gas circuit, raw material N
2storage tank is connected with blender by stop valve B, check valve B, threeway successively; The raw material storage tank on liquid charging stock liquid road is connected with blender by high pressure liquid phase Micro-metering Pumps, check valve C successively; Blender is connected with vaporizer, and vaporizer is connected with reactor; Reactor is connected with cooler tube side, and cooler tube side is connected with gas-liquid separator; The outlet of gas-liquid separator bottom liquid phases is connected with control valve A, sampler, control valve B in turn; Gas-liquid separator top gaseous phase outlet is connected with filter B, counterbalance valve, six-way valve and wet flow indicator in turn, and six-way valve is connected with gas-chromatography on-line analysis system simultaneously.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320735440.2U CN203620613U (en) | 2013-11-19 | 2013-11-19 | Heavy aromatics hydrogenation dealkylation lightweight reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320735440.2U CN203620613U (en) | 2013-11-19 | 2013-11-19 | Heavy aromatics hydrogenation dealkylation lightweight reaction device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203620613U true CN203620613U (en) | 2014-06-04 |
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ID=50807140
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320735440.2U Expired - Fee Related CN203620613U (en) | 2013-11-19 | 2013-11-19 | Heavy aromatics hydrogenation dealkylation lightweight reaction device |
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| CN (1) | CN203620613U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106179131A (en) * | 2016-06-27 | 2016-12-07 | 天津市鹏翔科技有限公司 | Liquid feedstock high efficient mixed system |
| CN107632098A (en) * | 2017-08-31 | 2018-01-26 | 天津市鹏翔科技有限公司 | Continuous catalytic reaction dynamic monitor |
| CN110187017A (en) * | 2019-05-09 | 2019-08-30 | 中触媒新材料股份有限公司 | A kind of propylene oxide on-line period device and method |
| CN111116327A (en) * | 2020-01-21 | 2020-05-08 | 山东玉皇化工有限公司 | Synthesis process of ethylene glycol mono-tert-butyl ether |
| CN113509888A (en) * | 2020-04-10 | 2021-10-19 | 中国石油化工股份有限公司 | Gas feed system |
| US11370973B2 (en) * | 2020-07-10 | 2022-06-28 | Saudi Arabian Oil Company | Processes and systems for producing one or more of benzene, toluene, or mixed xylenes |
-
2013
- 2013-11-19 CN CN201320735440.2U patent/CN203620613U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106179131A (en) * | 2016-06-27 | 2016-12-07 | 天津市鹏翔科技有限公司 | Liquid feedstock high efficient mixed system |
| CN107632098A (en) * | 2017-08-31 | 2018-01-26 | 天津市鹏翔科技有限公司 | Continuous catalytic reaction dynamic monitor |
| CN110187017A (en) * | 2019-05-09 | 2019-08-30 | 中触媒新材料股份有限公司 | A kind of propylene oxide on-line period device and method |
| CN111116327A (en) * | 2020-01-21 | 2020-05-08 | 山东玉皇化工有限公司 | Synthesis process of ethylene glycol mono-tert-butyl ether |
| CN113509888A (en) * | 2020-04-10 | 2021-10-19 | 中国石油化工股份有限公司 | Gas feed system |
| US11370973B2 (en) * | 2020-07-10 | 2022-06-28 | Saudi Arabian Oil Company | Processes and systems for producing one or more of benzene, toluene, or mixed xylenes |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140604 Termination date: 20211119 |