CN108299142A - A kind of energy-saving method of catalysis drying gas ethylbenzene - Google Patents
A kind of energy-saving method of catalysis drying gas ethylbenzene Download PDFInfo
- Publication number
- CN108299142A CN108299142A CN201711417507.7A CN201711417507A CN108299142A CN 108299142 A CN108299142 A CN 108299142A CN 201711417507 A CN201711417507 A CN 201711417507A CN 108299142 A CN108299142 A CN 108299142A
- Authority
- CN
- China
- Prior art keywords
- benzene
- tower
- ethylbenzene
- pressure
- column
- 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.)
- Withdrawn
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The present invention provides a kind of energy-saving methods of catalysis drying gas process for preparing ethylbenzene, recycle benzene needed for hydrocarbonylation, dealkylation reaction is used to be produced jointly by crude tower side line, benzene column side line, it is individually produced by benzene column side line in the former technological process of substitution, 120 DEG C ~ 140 DEG C of crude tower side take-off temperature, 0.55 ~ 0.85MPa of side take-off pressure（G）, 160 DEG C ~ 200 DEG C of benzene column side take-off temperature, 0.6 ~ 1.5MPa of side take-off pressure（G）, two towers, which are all made of the temperature difference and control, ensures recycle benzene purity；New process is using the former single column flow of ethylbenzene double tower differential pressure coupling flow substitution, including high-pressure tower（0.7~1.0MPa（G））, atmospheric tower（0.2~0.4MPa（G））, normal pressure tower bottom reboiler is heated using high pressure tower overhead gas as heat source, double tower can guarantee ethylbenzene yield and purity.Energy consumption significant effect of the present invention to reduction Benzene Device product separate section, it is contemplated that save Benzene Device energy 2.7~60.1 × 104Kcal/t ethylbenzene.
Description
Technical field
The present invention relates to catalysis drying gas to produce ethylbenzene technical field, and specifically there is provided a kind of catalysis drying gas ethylbenzene
Energy-saving method.
Background technology
Currently, China's energy resources face serious problem in short supply, waste is serious, unit GDP energy in 2004
Consumption is 3.1 times of world average level, is within 2012 2.5 times of world average level, it was reported that per Unit GDP Energy Consumption in 2015
Decline 5.6% than last year, but also has no small gap apart from world average level.Energy-saving is the important of enterprise's existence and development
The needs that energy-saving and emission-reduction are not only petroleum chemical industry self-growth are carried out in behave, and to promoting China's Resources for construction saving
Type and friendly environment society's important in inhibiting.
Styrene product is to synthesize the important monomer of high molecular material, and supply falls short of demand for domestic market, currently, the life of styrene
Produce the route country, foreign countries are all to be needed ethylbenzene as raw material based on ethylbenzene catalytic dehydrogenation, produced the technology path of ethylbenzene by original
Material is divided into pure ethylene ethylbenzene technology, dilute ethylbenzene manufactured from ethylene technology and C8 aronmatic separation production ethylbenzene technology, wherein with recycling
Utilize dilute ethylbenzene manufactured from ethylene technological process more economical rationality in refinery gas by-product dry gas.
Dry gas is present in as manufacture gas in refinery facilities, and wherein catalytic cracking unit generates dry large-minded, containing about
10~24（wt）% ethylene components, the technology for recycling this part ethylene both at home and abroad at present have dry gas legal system ethylbenzene, dry gas legal system
Aromatic naphtha, pressure-variable adsorption ethylbenzene.In 2004 by Fushun petrochemical industry designing institute invention disclosed, Patent No.
CN200410021102.8, it is detailed to describe catalysis drying gas process for preparing ethylbenzene flow, including feedstock processing, reaction, absorption, production
Product detach two parts, and absorption part therein is related to crude tower, and product separate section is related to benzene column, and plant energy consumption is 980,000 big
Card/ton ethylbenzene.2006, a kind of feedstock processing work of catalysis drying gas ethylbenzene is described in patent CN200610046750.8
Skill flow has been sloughed most MDEA, water and propylene, dry gas in dry gas and has been refined, and isopropylbenzene in reaction is reduced
Yield ensure that the production purity of rectifying separate section ethylbenzene.Facts proved that country's catalysis drying gas Benzene Device is effective at present
Combine the two technological processes, improve the output value of domestic Recovery rate of ethylene and ethylbenzene.
In previous catalysis drying gas process for preparing ethylbenzene, excessive benzene is big in reaction and piece-rate system as reaction raw materials
Amount cycle, the cycle approach for how optimizing and improving benzene will directly influence the energy consumption level of device.In Patent No.
In the invention of CN200410021102.8, with benzene individually by benzene column side take-off, excessive benzene is recycled in benzene column, is caused for reaction
Larger benzene column load also brings the increase of relevant device investment while increasing energy consumption.In addition, the flow of ethylbenzene single column,
Cause tower bottom reboiler load excessive.Therefore, in the energy-saving and emission-reduction policy of the keen competition and country that face chemical industry market
Under, it is necessary to the improvement that economy is made to current catalysis drying gas ethylbenzene technology, to save full device energy consumption.
Invention content
The object of the present invention is to provide a kind of energy-saving methods of catalysis drying gas process for preparing ethylbenzene, dry in previous catalysis
On the basis of gas process for preparing ethylbenzene flow, the technological process of product separate section is improved, reduces plant energy consumption 2.7~60.1
×104Kcal/t ethylbenzene reaches the floor level of domestic same device energy consumption.
Technical scheme of the present invention：
A kind of energy saving device of catalysis drying gas process for preparing ethylbenzene, including alkylation reaction device R1, dealkylation reaction device R2, cycle
Benzene heating furnace F, recycle benzene tank V1, reverse alkylation head tank V2, crude tower T1, hydrocarbonylation tail gas absorber T2, benzene column T3, ethylbenzene high pressure
Tower T4, ethylbenzene atmospheric tower T5；It is characterized in that：Increase crude tower side take-off benzene 6, the recycle benzene of extraction passes through flow control point
Two-way is used as alkylation reaction recycle benzene 4 after being mixed all the way to recycle benzene tank V1 with benzene column side take-off benzene 3 and supplement fresh benzene 2,
Temperature is 130 ~ 170 DEG C after mixed, and reaction temperature 290 ~ 360 is heated to through the preheating of alkylation reaction recycle benzene 4, recycle benzene heating furnace F
DEG C, from alkylation reaction device R1 at the top of enter fixed bed reactors, alkylation reaction product 4 through a series of heat exchange to 140 ~ 160 DEG C into
Enter crude tower T1 and carries out gas-liquid separation；All the way to reverse alkylation head tank V2 as dealkylation reaction recycle benzene 8, dealkylation reaction follows
Ring benzene 8 from crude tower side take-off benzene 6 mixed with the hydrocarbonylation absorption towers tail gas absorber T2 bottom rich absorbent after temperature be 110 ~
130 DEG C enter reverse alkylation head tank, and heat-exchange network is warming up to 260 DEG C into dealkylation reaction device R2 in device；Crude tower side
Line takes temperature control system, and the purity and mass flow of stringent control extraction benzene, the crude tower bottom material that flow is greatly reduced are made
It is fed for benzene column, enters benzene column after boosted, heat exchange.120 DEG C ~ 140 DEG C of crude tower side take-off temperature, side take-off pressure
0.55 ~ 0.85MPaG, 160 DEG C ~ 200 DEG C of benzene column side take-off temperature, 0.6 ~ 1.5MPaG of side take-off pressure.
（1）Crude tower side take-off is increased, the recycle benzene of extraction divides two-way by flow control, all the way to recycle benzene tank
It is used as alkylation reaction recycle benzene after being mixed with benzene column side take-off benzene and supplement fresh benzene, all the way to reverse alkylation head tank as anti-
Alkylation reaction recycle benzene, side line take temperature control system, the purity and mass flow of stringent control extraction benzene.Flow substantially drops
Low crude tower bottom material is fed as benzene column, enters benzene column after boosted, heat exchange.
（2）Benzene column side take-off benzene is not only re-used as reverse alkylation raw material as alkylation reaction raw material, until recycle benzene tank, half
Above recycle benzene is not recycled by being circulated between reaction system and crude tower after crude tower side take-off in benzene column, is reduced
Benzene column load.
（3）Benzene column reflux section and fixed gas are cooled to 40 DEG C, are emitted into the benzene/methylbenzene of fuel gas system or styrene units
Tower recycles benzene component.
（4）Flow is coupled using ethylbenzene tower double tower differential pressure, matches double tower inlet amount, ethylbenzene high pressure tower top oil gas is as warm
Source heats ethylbenzene normal pressure tower bottom reboiler, reduces overall load.
Previous process unit：
（1）Crude tower is fed without side take-off, materials at bottom of tower as benzene column, enters benzene column after boosted, heat exchange.
（2）Reaction with excessive recycle benzene only by benzene column side take-off, be circulated in reaction system and piece-rate system crude tower,
Benzene column.
（3）150 DEG C of benzene column reflux section and fixed gas enter crude tower, recycle the benzene component carried secretly in fixed gas；Or enter
Lights column removes light component, and is interrupted from return wire and liquid phase material is discharged, and removes non-aromatic component.
（4）Using ethylbenzene tower single column flow, tower overhead gas condensation while output low-pressure steam.
The advantageous effects of the present invention：
1, crude tower side take-off recycle benzene controls benzene purity 99.6wt% by the temperature difference.
2, the extraction of recycle benzene reduces the flow at crude tower bottom, reduces the shaft power of rough segmentation column bottoms pump.
3, crude tower side take-off benzene temperature is low 30 ~ 60 DEG C general compared with benzene column side take-off benzene temperature, and produced quantity is bigger
It is used as alkylation reaction recycle benzene, mixed rear temperature individually to be produced compared with benzene column anti-as hydrocarbonylation after benzene column produced quantity, two-way mixing
It answers the temperature of recycle benzene 20 ~ 40 DEG C low, reduces the bubble point pressure of recycle benzene, be conducive to the pressure control of recycle benzene tank, simultaneously
Improve the available NPSH of downstream recycle benzene pump；In addition recycle benzene Yu the reaction product heat exchange of lower temperature also improve dress
Internal heat energy utilization rate is set, heat-exchange network is optimized.
4, the reduction of rough segmentation materials at bottom of tower, that is, benzene column charging, significantly reduces the full tower load of benzene column, reduces correlation and set
Standby, pipeline investment.
5, the reduction of benzene column regurgitant volume reduces the shaft power of benzene column reflux pump.
6, benzene column reflux section and fixed gas are cooled to about 40 DEG C, reduce the content of non-aromatic component in fixed gas, avoid
Non-aromatic component is built up in systems.
7, ethylbenzene tower using high pressure, normal pressure double-column process, tower top output low-pressure steam, in single column ethylbenzene flow, output
Net energy about 18.7 × 104Kcal/t ethylbenzene, double-column process output net energy is about 37.1 × 104Kcal/t ethylbenzene, two kinds of flows
Scheme can save energy consumption~18.4 × 104Kcal/t ethylbenzene.It contributes for the energy consumption of whole device.
6, the methods for cooling of benzene column top gas can use production low-pressure steam according to the needs of different device, air cooling, follow
The scheme of ring water cooling is reduced benzene column top gas amount, is reached to three of the above cooling scheme due to the reduction of benzene column top load
Energy-saving effect comparing result be circulating water>Air cooling>Low-pressure steam is produced, i.e., only the cooling of benzene column top gas is come
It says, maximum can reduce energy consumption 5.03 × 104Kcal/t ethylbenzene, significant effect.
7, the reduction of benzene column bottom thermic load, with fuel gas convert energy consumption, benzene column bottom can reduce energy consumption about 36.4 ×
104Kcal/t ethylbenzene.
8, improved catalysis drying gas process for preparing ethylbenzene flow can save full device energy consumption 2.7~60.1 × 104Kcal/t second
Benzene improves the market competitiveness, has led the innovation of ethylbenzene technical field economic benefit.
Description of the drawings
Fig. 1 is reaction and product separation process schematic diagram in the energy-saving technique of catalysis drying gas ethylbenzene.
Wherein R1 is alkylation reaction device, and R2 is dealkylation reaction device, and F is recycle benzene heating furnace, and V1 is recycle benzene tank, and V2 is
Reverse alkylation head tank, T1 are crude towers, and T2 is absorption tower, and T3 is benzene column, and T4 is ethylbenzene high-pressure tower, and T5 is ethylbenzene atmospheric tower, and 1 is
Dry gas is purified, 2 be supplement fresh benzene, and 3 be benzene column side take-off benzene, and 4 be alkylation reaction product, and 5 be crude tower base oil, and 6 be thick
Divide tower side take-off benzene, 7 be benzene column base oil, and 8 be dealkylation reaction product, and 9 be the charging of ethylbenzene high-pressure tower, and 10 be ethylbenzene atmospheric tower
Charging.
Specific implementation mode
The present invention is realized by following specific technical solution：
Purification dry gas 1 divides four roads into alkylation reaction device R1, and fresh benzene 2, benzene column side take-off benzene 3, the crude tower side line of supplement are adopted
Go out benzene 6 and be mixed into recycle benzene tank V1, reaction temperature is heated to through the preheating of alkylation reaction product 4, recycle benzene heating furnace F, from hydrocarbon
Change and enters fixed bed reactors at the top of reactor R1.Alkylation reaction product 4 enters crude tower through a series of exchange heat to 140 ~ 160 DEG C
T1 carries out gas-liquid separation.
Crude tower T1 side take-offs benzene 6,120~140 DEG C of temperature control benzene purity 99.6wt% by the temperature difference, and pressure is
0.55~0.85MPaG；Gravity flow divides two-way to enter recycle benzene tank V1, reverse alkylation head tank V2 through pump boosting.It is fed in reverse alkylation
In tank, side take-off benzene from crude tower with after the absorption tower bottoms of tower T2 rich absorbent is boosted and preheating into reverse alkylation
Reactor R2.Dealkylation reaction product 8 and crude tower T1 bottom of tower oil enter benzene column as benzene column charging.Benzene column side take-off benzene,
160~200 DEG C of temperature, until recycle benzene tank V1 and crude tower side take-off benzene, supplement fresh benzene mix after 130~170 DEG C of temperature,
As alkylation reaction recycle benzene.Benzene column top gas cooling for reflux needs that different cooling schemes can be used according to device；Saturation is steamed
Vapour, using circulating water, using air cooling, it is horizontal that different schemes will influence plant energy consumption.Benzene column base oil 7 is used as ethylbenzene tower
Charging is divided to two strand 9 and 10 to respectively enter ethylbenzene high-pressure tower T4 and ethylbenzene atmospheric tower T5,0.7 ~ 1.0MPaG of ethylbenzene high pressure pressure tower,
200 ~ 240 DEG C of tower top temperature, 0.2 ~ 0.4MPaG of ethylbenzene normal pressure pressure tower, 200 ~ 230 DEG C of column bottom temperature, ethylbenzene high pressure tower overhead gas
As ethylbenzene normal pressure tower bottom reboiler heat source, carries out differential pressure with ethylbenzene atmospheric tower and couple, the ethylbenzene production of two tower overhead gases after cooling
Product enter next unit after converging, and two materials at bottom of tower are through converging to propyl benzene tower.
Claims (3)
1. a kind of energy saving device of catalysis drying gas process for preparing ethylbenzene, including alkylation reaction device（R1）, dealkylation reaction device
（R2）, recycle benzene heating furnace（F）, recycle benzene tank（V1）, reverse alkylation head tank（V2）, crude tower（T1）, hydrocarbonylation tail gas absorber
（T2）, benzene column（T3）, ethylbenzene high-pressure tower（T4）, ethylbenzene atmospheric tower（T5）；It is characterized in that：Increase crude tower side take-off benzene
（6）, the recycle benzene of extraction divides two-way by flow control, all the way to recycle benzene tank（V1）With benzene column side take-off benzene（3）And it mends
Fill fresh benzene（2）Alkylation reaction recycle benzene is used as after mixing（4）, temperature is 130 ~ 170 DEG C after mixing, through alkylation reaction recycle benzene
（4）Preheating, recycle benzene heating furnace（F）It is heated to 290 ~ 360 DEG C of reaction temperature, from alkylation reaction device（R1）Top enters fixed bed
Reactor, alkylation reaction product（4）Enter crude tower to 140 ~ 160 DEG C through exchanging heat（T1）Carry out gas-liquid separation；All the way to anti-hydrocarbon
Change head tank（V2）As dealkylation reaction recycle benzene（8）, dealkylation reaction recycle benzene（8）From crude tower side take-off benzene
（6）With hydrocarbonylation tail gas absorber（T2）Temperature enters reverse alkylation head tank for 110 ~ 130 DEG C after the rich absorbent mixing of absorption tower bottom,
Heat-exchange network is warming up to 260 DEG C into dealkylation reaction device in device（R2）；Crude tower side line takes temperature control system, sternly
The purity and mass flow of lattice control extraction benzene, the crude tower bottom material that flow is greatly reduced are fed as benzene column, boosted, heat exchange
Enter benzene column afterwards.
2. a kind of energy saving device of catalysis drying gas process for preparing ethylbenzene according to claim 1, it is characterised in that：Rough segmentation
120 DEG C ~ 140 DEG C of tower side take-off temperature, 0.55 ~ 0.85MPa of side take-off pressure（G）, 160 DEG C of benzene column side take-off temperature ~
200 DEG C, 0.6 ~ 1.5MPa of side take-off pressure（G）.
3. a kind of energy saving device of catalysis drying gas process for preparing ethylbenzene according to claim 1, it is characterised in that：Using
Ethylbenzene double tower differential pressure couples the former single column flow of flow substitution, benzene column base oil（7）It is divided to two strands of ethylbenzene high-pressure towers as ethylbenzene tower charging
Charging（9）It is fed with ethylbenzene atmospheric tower（10）, respectively enter ethylbenzene high-pressure tower（T4）With ethylbenzene atmospheric tower（T5）, ethylbenzene high-pressure tower
0.7 ~ 1.0MPa of pressure（G）, 200 ~ 240 DEG C of tower top temperature, 0.2 ~ 0.4MPa of ethylbenzene normal pressure pressure tower（G）, column bottom temperature 200 ~
230 DEG C, ethylbenzene high pressure tower overhead gas carries out differential pressure as ethylbenzene normal pressure tower bottom reboiler heat source, with ethylbenzene atmospheric tower and couples, two towers
The ethylbenzene product of top gas after cooling enters next unit after converging, and two materials at bottom of tower are through converging to propyl benzene tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711417507.7A CN108299142A (en) | 2017-12-25 | 2017-12-25 | A kind of energy-saving method of catalysis drying gas ethylbenzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711417507.7A CN108299142A (en) | 2017-12-25 | 2017-12-25 | A kind of energy-saving method of catalysis drying gas ethylbenzene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108299142A true CN108299142A (en) | 2018-07-20 |
Family
ID=62871012
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711417507.7A Withdrawn CN108299142A (en) | 2017-12-25 | 2017-12-25 | A kind of energy-saving method of catalysis drying gas ethylbenzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108299142A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110776391A (en) * | 2019-11-11 | 2020-02-11 | 山东京博石油化工有限公司 | Device and method for preparing ethylbenzene from dry gas |
| CN113024339A (en) * | 2021-01-15 | 2021-06-25 | 宁波科元精化股份有限公司 | Production process for reducing liquid carried in hydrocarbon tail gas of ethylbenzene device |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1557794A (en) * | 2004-02-02 | 2004-12-29 | 抚顺石油化工设计院 | Technological process for catalyzing dry gas to prepare ethylbenzene |
| CN1749227A (en) * | 2005-10-19 | 2006-03-22 | 大连理工大学 | Energ ysaving method for producing ethyl benzene by benzene and dry gas hydrocarbonization |
| CN101602640A (en) * | 2008-06-12 | 2009-12-16 | 中国石油化工股份有限公司 | The energy-saving separation method of ethyl benzene/styrene |
| CN101768043A (en) * | 2008-12-31 | 2010-07-07 | 中国科学院大连化学物理研究所 | Method for preparing ethylbenzene by reaction of dilute ethylene and benzene |
| CN104341264A (en) * | 2013-08-08 | 2015-02-11 | 中石化洛阳工程有限公司 | Separation process for producing ethylbenzene and/or propylbenzene product from gas containing ethylene and/or propylene by gas phase process |
| CN105669352A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Ethylbenzene/styrene energy-saving separation method |
-
2017
- 2017-12-25 CN CN201711417507.7A patent/CN108299142A/en not_active Withdrawn
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1557794A (en) * | 2004-02-02 | 2004-12-29 | 抚顺石油化工设计院 | Technological process for catalyzing dry gas to prepare ethylbenzene |
| CN1749227A (en) * | 2005-10-19 | 2006-03-22 | 大连理工大学 | Energ ysaving method for producing ethyl benzene by benzene and dry gas hydrocarbonization |
| CN101602640A (en) * | 2008-06-12 | 2009-12-16 | 中国石油化工股份有限公司 | The energy-saving separation method of ethyl benzene/styrene |
| CN101768043A (en) * | 2008-12-31 | 2010-07-07 | 中国科学院大连化学物理研究所 | Method for preparing ethylbenzene by reaction of dilute ethylene and benzene |
| CN104341264A (en) * | 2013-08-08 | 2015-02-11 | 中石化洛阳工程有限公司 | Separation process for producing ethylbenzene and/or propylbenzene product from gas containing ethylene and/or propylene by gas phase process |
| CN105669352A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Ethylbenzene/styrene energy-saving separation method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110776391A (en) * | 2019-11-11 | 2020-02-11 | 山东京博石油化工有限公司 | Device and method for preparing ethylbenzene from dry gas |
| CN110776391B (en) * | 2019-11-11 | 2022-05-31 | 山东京博石油化工有限公司 | Device and method for preparing ethylbenzene from dry gas |
| CN113024339A (en) * | 2021-01-15 | 2021-06-25 | 宁波科元精化股份有限公司 | Production process for reducing liquid carried in hydrocarbon tail gas of ethylbenzene device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101570466B (en) | Multi-effect rectifying process of methanol | |
| CN202808649U (en) | Systemic device for preparing polyoxymethylene dimethyl ether | |
| CN102701923B (en) | System device and process for preparing polymethoxy dimethyl ether | |
| CN105837389B (en) | A kind of heat-exchange network for the method and this process for producing paraxylene | |
| CN209113783U (en) | A kind of separation system using divided wall column separating high-purity isopentane and pentane | |
| CN102321059B (en) | Production process and production device of phthalic anhydride | |
| CN1319915C (en) | Energ ysaving method for producing ethyl benzene by benzene and dry gas hydrocarbonization | |
| CN104513159A (en) | Butyl acetate energy saving production method | |
| CN108299142A (en) | A kind of energy-saving method of catalysis drying gas ethylbenzene | |
| CN205398514U (en) | Cyclohexanone refining plant in cyclohexanone production process | |
| CN109761735A (en) | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH | |
| CN219209011U (en) | Nitroamine hydrogenation reaction thermal cycle recycling system | |
| CN105566030A (en) | Method for separating BTX | |
| CN106608833B (en) | Ethanol amine co-production | |
| CN109536204B (en) | Catalytic cracker for low-temp. heat upgrading | |
| CN218306233U (en) | Energy-saving separation device for sulfuric acid alkylation reaction product | |
| CN102701899A (en) | Energy conservation and emission reduction process for producing p-xylene through alkylation of tolylcarbinol | |
| CN109351289A (en) | A method of control alkylation reactor bed temperature rise | |
| CN101260036B (en) | Modified technique for refined unit in acrylic acid production device | |
| CN104801249A (en) | Method for recycling energy in oxo synthesis device | |
| CN204503035U (en) | High Efficiency Thermal integrated-type moving bed Methanol hydrocarbon system | |
| CN208414288U (en) | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide | |
| CN104844402B (en) | Efficient heat-integrated method for preparing hydrocarbon from methanol by adopting moving bed | |
| CN204848758U (en) | Remove bed methyl alcohol system hydrocarbon system all | |
| CN104725181B (en) | Initial separation technique of gas generated by reaction for preparing propylene from oxygen-containing compounds |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WW01 | Invention patent application withdrawn after publication | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20180720 |