CN1923973A - Process flow for raw material pretreatment portion of catalytic dry gas produced phenylethane - Google Patents
Process flow for raw material pretreatment portion of catalytic dry gas produced phenylethane Download PDFInfo
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- CN1923973A CN1923973A CN 200610046750 CN200610046750A CN1923973A CN 1923973 A CN1923973 A CN 1923973A CN 200610046750 CN200610046750 CN 200610046750 CN 200610046750 A CN200610046750 A CN 200610046750A CN 1923973 A CN1923973 A CN 1923973A
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Abstract
The invention discloses a predisposing technological flow path of ethylbenzene through catalyzing dried gas, which comprises the following steps: adsorbing propylene; desorbing ethylene; desorbing propylene; adding raw material to strip propylene; washing most of MEDA; entering standard dried gas in the delivery tank; entering into propylene adsorbing tower; draining purified dried gas from top of propylene adsorbing tower; making one path as cool material in the ethylene stripping tower and one path to exchange heat with base material of propylene stripping tower under 10-300 deg.c in the ethylene stripping tower; desorbing ethylene component; draining ethylene gas; returning in the dried gas delivery tank; circulating between ethylene stripping tower and propylene stripping tower; desorbing propylene component from adsorbant with 150ppm-0.7% dried propylene in the stripped propylene.
Description
Technical field:
The present invention relates to refinery gas recovery technology field in the petrochemical complex, exactly it is a kind of absorption desorption technique flow process a---process flow for raw material pretreatment portion of catalytic dry gas produced phenylethane.
Background technology:
Refinery gas is that each process unit institute aerogenesis body (comprises hydrogen and C in the petroleum refining process
1To C
4Alkane, alkene and a small amount of C
5) general name.The device that produces refinery gas mainly comprises hot procedures such as primary distillation of crude oil, catalytic cracking, hydrocracking and coking, viscosity breaking.The method of industrial general employing absorption and desorb in the gas greater than C
3And less than C
2Component carry out Separation and Recovery, promptly be the absorption desorption process that is adopted in the general refinery.
What absorb the extensive employing at present of desorption technique flow process has two types, and single tower absorbs the desorb flow process and double tower absorbs the desorb flow process.The former characteristics are that absorption process adopts an absorption-desorption tower, make greater than C
3The absorption of component and less than C
2The desorption process of component carries out in same absorption-desorption tower.The latter's characteristics are that absorption and desorption are carried out in two towers, have solved single tower flow process and have absorbed and the mutual interference problem of desorption process in same tower.The yield of single tower flow process liquid hydrocarbon has only 60～70%, and double-column process then can reach 95%.University Of Tianjin has applied for a patent of invention in 2005, the patent No. is: CN200510014443.7, name is called the patent of invention of " stepwise condensation process for catalytic cracking absorbing-stabilizing system and recombining process thereof ", adopt double-column process, to compress and directly enter surge tank after rich gas, rich absorbent oil and stripping gas mix and carry out gas-liquid separation, and then substep cools off condensed oil and non-condensable gas, enter the middle and upper part of desorption tower after condensed oil cools off a little as hot feed, and non-condensable gas is cooled to enter the desorption tower top as cold feed behind the lesser temps.Anqing Petro-Chemical General Plant, China Petro-Chemical Corp. has applied for the patent of invention of " a kind of absorption stabilizing process for refining oil " in calendar year 2001, the patent No. is: CN01117638.5, what adopt also is double-column process, it is with process pressure-raising and refrigerative rich gas, rich absorbent oil at the bottom of the absorption Tata, the stripping gas of desorb cat head mixes back condensation cooling and enters oil-gas separator, gas phase partly enters the bottom, absorption tower, liquid phase part heats up through heat exchange and enters the desorption tower top, it is installing under the motionless situation of most equipment, can obviously improve unit capacity, under the constant situation of treatment capacity, can reduce plant energy consumption, improve the quality of products.South China Science ﹠ Engineering University has applied for a patent of invention in 1999, the patent No. is: CN99116296.X, name is called the patent of invention of " absorption stabilizing apparatus for catalytic cracking and technical process thereof ", adopt single tower flow process, if an oil absorbs deethanizing column, cat head is provided with a condenser system, and tower first half rectifying section is provided with one or two component cooling system, tower Lower Half stripping section is provided with an intermediate reboiler system, is provided with a tower still reboiler at the bottom of the tower.It has cancelled return material, improved product recovery rate suitable with material quantity of two plume amounts of existing apparatus, has reduced by-product volume and process cost.
Begin just to have adopted double-column process latter stage from the fifties abroad.The most of employing of domestic gas concentration unit absorbs the double-column process of installing respectively with desorption tower.The pressure range on absorption tower is in 0.7～2.1MPa (gauge pressure), and the temperature range of employing generally is controlled at about 40 ℃ at 32～49 ℃.External some device absorptive tower temperature is low to reach 10 ℃, absorbs at low temperatures, and the rate of recovery of propylene can reach more than 95%.Many refineries, replenish with the debutylize catalytically cracked gasoline as oil-poor with the catalytically cracked gasoline of debutylize not, and the propylene rate of recovery reaches 90%, and butylene reaches more that the heavy constituent yield reaches 99%.Adopt the oil-poor of lower molecular weight, can reduce oil-poor internal circulating load.It is documented that oil-poor molecular weight cans be compared to big 3～4 carbon of component of required absorption most.The patent " a kind of absorption process of refrigeration oil " of Xi'an Changqing Technology Engineering Co., Ltd's application, patent No. CN200410073169.6, it is to install the refrigeration oil absorption process that self-produced stable light hydrocarbon is an absorption agent, can be with less absorption agent, obtain higher light hydrocarbon recovery rate, be applicable to and reclaim liquefied gas and C from associated gas or from Sweet natural gas
3The recovery technology that yield is had relatively high expectations.Dalian Inst of Chemicophysics, Chinese Academy of Sciences has applied for the patent of a key name for " a kind of method of selecting to absorb propylene in the reduction catalytic cracked dry gas ", the patent No.: CN200410037433.0, it absorbs propylene in the dry gas with absorption agent, with sweeping gas the absorption agent that is absorbed with propylene is carried out desorb then, the absorption agent after the desorb can be recycled.
Catalytic cracked dry gas is as the preparing ethylbenzene from dry gas raw material, and density of propylene is everlasting about 3%, in the alkylation reaction of ethene and benzene, follows the side reaction of propylene and benzene, and the generation of by product propyl benzene not only influences the purity of ethylbenzene product, and has increased the benzene consumption.Experiment showed, that propylene content can effectively suppress the generation of propylene and benzene side reaction below 0.7% in the control dry gas.
Summary of the invention:
The purpose of this invention is to provide a kind of catalysis drying gas system ethylbenzene raw material pretreatment process flow process, it can be controlled effectively, and propylene content can effectively suppress the generation of propylene and benzene side reaction below 0.7% in the dry gas.
It comprises the propylene absorption portion, takes off ethylene moiety and takes off the propylene part, it is characterized in that: catalysis drying gas enters dry gas and divides flow container (2) to enter propylene absorption tower (4) after MDEA is deviate from water wash column (1) washing, and absorption agent enters propylene absorption tower (4) after extracting deep cooling out by pump in the absorption agent jar (3).Catalysis drying gas and top-down absorption agent counter current contact after absorption agent has absorbed the propylene component in the dry gas, purify dry gas and absorb the cat head discharge from propylene, and the bottoms material is extracted out by pump, divides two-way to enter and takes off ethylene column (4).One the tunnel directly enters depropenizer (5) as cold feed, and one the tunnel takes off ethylene column (5) as entering after hot feed and the heat exchange of depropenizer substrate material.Absorption agent is separated sucking-off ethylene component wherein in taking off ethylene column (5), the circulation dry gas is discharged from taking off the ethene cat head, is back to and enters propylene absorption tower (4) after dry gas divides flow container (2) separatory.Take off ethylene column substrate material from compressing into, separate sucking-off propylene component wherein into depropenizer (6).Enter depropenizer top return tank (7) after the oil gas condensation cooling of depropenizer top, behind the gas phase part deep cooling, non-condensable gas enters fuel gas and divides flow container as fuel in the device, and liquid phase is from flowing back to depropenizer top return tank (7).After being extracted out by pump, depropenizer top return tank (7) liquid returns the depropenizer top as phegma.Depropenizer substrate material with take off ethylene column hot feed heat exchange after enter circulation absorption agent jar (3), mixes the back with additional absorption agent in the use of system internal recycle.
In the above-mentioned technical process:
1) adopt benzene to make absorption agent, the volume ratio of absorption agent and dry gas is 2～30;
2) absorption agent after the desorb can use at system's internal recycle, and the purity of benzene should reach 95～99%;
3) two desorption towers are established in two sections desorbs.First section desorb ethylene component, second section desorb propylene component;
4) first section stripping gas be at system's internal recycle, 0～300 ℃ of desorption temperature, desorption pressures 0.1～4.0MPa;
5) low temperature absorption, acceptance condition: service temperature-20～60 ℃, pressure 0.1～4.0MPa;
6) the depropenizer charging has hot and cold two bursts of chargings, and feeding temperature is 0～200 ℃; Cat head is not established water cooler, and tower top temperature is regulated by the cold feed amount, desorption temperature-10～200 ℃, desorption pressures 0.1～4.0MPa.
Advantage of the present invention is:
The raw material treating part of technology was a dry gas after desulfurization, washing in the past, directly entered reactive system.
The present invention: the raw material dry gas, after one section absorption, two sections desorbs, removed propylene component wherein, take off propylene after dry gas third rare content have only 150ppm～0.7%, effectively reduced the generation of propylene and benzene side reaction, reduced the benzene consumption.Concrete characteristics are as follows:
1) the used absorption agent of the present invention is a benzene, and benzene is one of device raw material, saves a large amount of absorption agents;
2) the present invention adopts low temperature absorption technology, and the absorption agent deep cooling more helps absorbing to-10～40 ℃;
3) the present invention adopts two sections desorption techniques, and yield of ethene can reach 98～99%, and the propylene decreasing ratio can reach more than 95～98%;
4) the present invention takes off the ethene cat head and does not establish water cooler, and depropenizer top temperature is regulated by the cold feed amount.
Characteristics of the present invention and positively effect can be embodied from following application example.
Description of drawings
Fig. 1 is catalysis drying gas system ethylbenzene raw material pretreatment process schematic flow sheet.
As shown in the figure: the 1st, water wash column, the 2nd, dry gas divides flow container, and the 3rd, the absorption machine jar, the 4th, the propylene absorption tower, the 5th, take off ethylene column, 6 depropenizers, the 7th, depropenizer top return tank.
Embodiment:
Equipment among the present invention all is the equipment that uses in the existing technology, all can order or purchase.Different among the present invention according to instrument size benzene absorption agent consumption, but the volume ratio that guarantees absorption agent and dry gas is 2～30 to get final product.
0.6～1.0MPa, 40 ℃ catalysis drying gas enter water wash column 1 washing from system, washing water is that fresh water recycles (wherein having additional), deviates from most of MDEA in the dry gas, and the dry gas MDEA concentration after the washing is reduced to below the 1PPM.Dry gas after the washing enters dry gas and divides flow container 2 and take off that ethylene column 5 top circulation dry gas mix after residue gas compressor compression back enters propylene absorption tower 4 1.2～1.4MPa, 40 ℃.Dry gas after cat head purifies enters the alkylation reaction device after 1.2MPa, 15 ℃ and ethylbenzene product heat exchange to 126 ℃.Rich absorbent enters through pump pressurization back branch two-way 1.25MPa, 22.5 ℃ and takes off ethylene column 5 at the bottom of 4 towers of propylene absorption tower, one road cold feed directly enters 1.67MPa, 22.5 ℃ and takes off the ethene cat head, enters after the poor absorption agent heat exchange to 120 ℃ at the bottom of another road and the depropenizer and takes off ethylene column 5.Take off the ethylene column overhead gas and return the suction port of compressor 1.0MPa, 40 ℃ and divide flow container, liquid enters depropenizer 1.02MPa, 168 ℃ at the bottom of the tower.Depropenizer top oil gas enters depropenizer top return tank 7 0.35MPa, 100 ℃ after condensation is cooled to 40 ℃, gas phase part deep cooling to 10 ℃, gas phase wherein is rich propylene dry gas, enter fuel gas and divide flow container 0.3MPa, 10 ℃ as this unit furnace fuel, liquid phase is from flowing back to depropenizer top return tank, extract the back out by pump and return cat head as phegma 0.76MPa, 40 ℃, stripping liquid ℃ returns the absorption agent jar in 0.4MPa, 131 ℃ and liquid heat exchange to 40 at the bottom of the propylene absorption tower at the bottom of the tower, returns the propylene absorption tower as the circulation absorption agent.
Claims (2)
1, process flow for raw material pretreatment portion of catalytic dry gas produced phenylethane, it comprises that propylene absorbs, ethene desorb and propylene desorb three parts, it is characterized in that: what increase raw material before reactive moieties takes off propylene technology, through the catalysis drying gas of desulfurization behind system's access to plant, be introduced into the water wash column washing, deviate from most of MDEA wherein, dry gas after the washing is reduced to MDEA concentration below the 1PPM, after qualified dry gas advances minute flow container separatory, enter the propylene absorption tower, with the absorption agent counter current contact that is cooled to-10～40 ℃ from top to bottom, wherein propylene component and part ethylene component absorbed; Purify dry gas and absorb the cat head discharge from propylene, divide three the tunnel to advance the alkylation reaction device, propylene absorption tower substrate material one the tunnel directly enters as cold feed and to take off ethylene column after pump pressurization, one the tunnel enters as hot feed with depropenizer substrate material heat exchange to 10～about 300 ℃ and to take off ethylene column, ethylene component is wherein desorbed, ethylene-rich gas is discharged from taking off the ethene cat head, returning dry gas divides behind the flow container separatory on the propylene absorption tower and takes off between the ethylene column and circulate, take off ethylene column substrate material from being depressed into depropenizer, propylene component in the absorption agent is desorbed, overhead oil air cooling enters the depropenizer return tank of top of the tower after coagulating cooling, phlegma is squeezed into the depropenizer cat head as backflow, non-condensable gas enters condenser condenses to-10～200 ℃, rich propylene gas is discharged from cat head, as fuel in the device, liquid phase is from flowing into the depropenizer return tank of top of the tower, poor absorption agent of depropenizer bottoms material and the substrate material heat exchange to 10 of propylene absorption tower～about 200 ℃ backs are from being depressed into the absorption agent jar, absorption agent is extracted out from the absorption agent jar again, enters the propylene absorption tower through pump pressurization postcooling to-10～40 ℃ and recycles.
2, catalysis drying gas system ethylbenzene raw material pretreatment process according to claim 1 is characterized in that:
1) absorption agent adopts benzene in the technology, and the volume ratio of absorption agent and dry gas is 2～30;
2) absorption agent after the desorb can use at system's internal recycle, and the purity of benzene should reach 95～99%;
3) two desorption towers are established in two sections desorbs, first section desorb ethylene component, second section desorb propylene component;
4) first section stripping gas be at system's internal recycle, 0～300 ℃ of desorption temperature, desorption pressures 0.1～4.0MPa;
5) low temperature absorption, acceptance condition: service temperature-20～60 ℃, pressure 0.1～4.0MPa;
6) the depropenizer charging has hot and cold two bursts of chargings, and feeding temperature is 0～200 ℃; Cat head is not established water cooler, and tower top temperature is regulated by the cold feed amount, desorption temperature-10～200 ℃, desorption pressures 0.1～4.0MPa.
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| CN101659589A (en) * | 2009-09-15 | 2010-03-03 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN101659590A (en) * | 2009-09-15 | 2010-03-03 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN101665396A (en) * | 2009-09-15 | 2010-03-10 | 中国石油化工集团公司 | Refining method of virgin gas containing ethane used in process for preparing ethylbenzene by ethane |
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| CN101768043B (en) * | 2008-12-31 | 2013-09-25 | 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 |
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| CN115304448A (en) * | 2022-07-21 | 2022-11-08 | 中石化广州工程有限公司 | Process and device for preparing ethylbenzene by ethylene-containing dry gas-liquid phase method |
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| CN101768043B (en) * | 2008-12-31 | 2013-09-25 | 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 |
| CN101665397B (en) * | 2009-09-15 | 2013-07-10 | 中国石油化工集团公司 | Refining method of propylene containing ethane used in process for preparing ethylbenzene by ethane |
| CN101659590A (en) * | 2009-09-15 | 2010-03-03 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN101665396A (en) * | 2009-09-15 | 2010-03-10 | 中国石油化工集团公司 | Refining method of virgin gas containing ethane used in process for preparing ethylbenzene by ethane |
| CN101659589A (en) * | 2009-09-15 | 2010-03-03 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN101665396B (en) * | 2009-09-15 | 2013-01-02 | 中国石油化工集团公司 | Refining method of virgin gas containing ethane used in process for preparing ethylbenzene by ethane |
| CN101659589B (en) * | 2009-09-15 | 2013-01-02 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN101906319A (en) * | 2010-08-10 | 2010-12-08 | 华南理工大学 | Method for pre-processing raw materials for catalytic reforming device and device thereof |
| CN101906319B (en) * | 2010-08-10 | 2013-04-17 | 华南理工大学 | Method for pre-processing raw materials for catalytic reforming device and device thereof |
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| CN106588557A (en) * | 2017-01-13 | 2017-04-26 | 山东京博石油化工有限公司 | Method for preparing ethylbenzene from refinery dry gas |
| CN106588557B (en) * | 2017-01-13 | 2019-04-19 | 山东京博石油化工有限公司 | A kind of method that oil refinery dry gas prepares ethylbenzene |
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| CN115304448A (en) * | 2022-07-21 | 2022-11-08 | 中石化广州工程有限公司 | Process and device for preparing ethylbenzene by ethylene-containing dry gas-liquid phase method |
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Owner name: LIAONING BRANCH OF CHINA HUANQIU CONTRACTING + ENG Free format text: FORMER NAME: FUSHUN BRANCH, CHINA PETROLEUM GROUP ENGINEERING DESIGN CO., LTD. |
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Address after: 113006 Liaoning province Fushun City River Road No. 16 Patentee after: Liaoning Branch,China Huanqiu Engineering Co., Ltd. Address before: 113006 Liaoning province Fushun City River Road No. 16 Patentee before: Fushun Branch, China Petroleum Group Engineering Design Co., Ltd. |