CN103159581A - System and method for preparing polymer-grade propylene through absorption and separation of catalytic cracking product gas - Google Patents
System and method for preparing polymer-grade propylene through absorption and separation of catalytic cracking product gas Download PDFInfo
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- CN103159581A CN103159581A CN2011104125144A CN201110412514A CN103159581A CN 103159581 A CN103159581 A CN 103159581A CN 2011104125144 A CN2011104125144 A CN 2011104125144A CN 201110412514 A CN201110412514 A CN 201110412514A CN 103159581 A CN103159581 A CN 103159581A
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Abstract
The invention provides a system and a method for preparing polymer-grade propylene through absorption and separation of catalytic cracking product gas. A debutanizing tower, an absorption tower, and a desorption tower are sequentially arranged between a pre depropanizing tower and a post depropanizing tower. A propylene tower is arranged behind the post depropanizing tower. A gas enrichment balancing tank is arranged between the absorption tower and the desorption tower. Through the pre depropanizing tower, catalytic cracking product gas is separated into C3 and lighter components and C4 and heavier components. The C4 and heavier components are processed by using the debutanizing tower, such that C4 component or C5 and heavier components are obtained. The obtained component is adopted as an absorption agent, and is used for absorbing the C3 and lighter components of the pre depropanizing tower top gas in the absorption tower. With the desorption tower, C3 component and C2 and lighter components are separated through desorption. The tower kettle liquid of the desorption tower is delivered to the post depropanizing tower. Post depropanizing tower top gas is subjected to propane-propylene separation in the propylene tower, such that the polymer-grade propylene product is obtained at the top of the propylene tower. With the system and method provided by the invention, an oil absorption method is adopted; the application of low-temperature cold energy is avoided; energy consumption is reduced; and equipment investment is saved.
Description
Technical field
The present invention relates to the oily method for absorbing and separating of catalytic cracking reaction gas product.More particularly, relate to the system and method that replaces the absorption extraction catalytic pyrolysis gas product polymerization-grade propylene processed of traditional cryogenic rectification partition method with oil-absorption process.
Background technology
Mainly contain methane, carbon two, carbon three, carbon four and carbon five and more the catalytic cracking reaction gas product of heavy constituent generally by supercharging and adopt traditional cryogenic rectification separation method of cryogenic coolant condensation to separate.usually Fig. 1 is seen in the technical process of the method, be at first with the catalytic pyrolysis gas product with the first compressor P1, be compressed to 1.0MPa-1.6MPa, then lime set between gas phase and compressor section is delivered to depropanizing tower P2, with carbon three and more light constituent and carbon four and more heavy constituent separate, reaching carbon three more again, light constituent is compressed to 3.4MPa-4.0MPa with the second compressor P3, deliver to ethylene column P5 and remove carbon two and light constituent more, carbon three components of tower reactor are delivered to propylene tower P6 again, separation of propylene and propane, obtain the polymerization-grade propylene monomer, carbon four and more heavy constituent deliver to debutanizing tower P4 and separate, acquisition carbon four and carbon five reach more heavy constituent (raw pyrolysis gasoline).The separation method energy consumption of this routine is higher and facility investment is also higher, reason is: carbon three and more light constituent need compress and just can enter ethylene column and separate, energy consumption is higher, and needs to increase a compressor or increase special compression section on the gas product compressor, and facility investment increases; Simultaneously, the ethene tower top need adopt the cryogen condensation of-15 ℃, and the cryogen power consumption is high, if freezing unit is set separately, plant investment increases.
CN 101234946A discloses a kind of separation method of low-carbon olefin mixed gas, comprise the steps: and to pass into compensation tower or surge tank through the cooling low-carbon olefin mixed gas of heat exchange, the gas of collecting from the top of described compensation tower or surge tank passes into the absorption tower, pass into absorption agent from top, described absorption tower, through mass transfer, be not absorbed C2 that agent absorbs and more light constituent collect from the top on described absorption tower, treat that absorbent regeneration is from the bottom described compensation tower of input or the surge tank on absorption tower, after mass transfer, bottom output by described compensation tower or surge tank enters the one-level desorption tower again, after the desorb mass transfer, with the C2 component gas described compensation tower of input of described one-level desorption tower top collection or the bottom of surge tank, liquid input secondary desorption tower with described one-level desorption tower bottom, through the desorb mass transfer, the liquid that described secondary desorption tower top is collected is input to and takes off the C3 tower, after the described material process mass transfer that takes off in the C3 tower, the liquid that the described C3 of taking off top of tower is collected inputs to the C3 knockout tower, separate through mass transfer, collect from the top of the described C3 of taking off tower and obtain propylene, collect from the bottom of the described C3 of taking off knockout tower and obtain propane, the liquid of the described C3 of taking off tower bottom is input to takes off the absorption agent tower, collect the described absorption agent column overhead of taking off to such an extent that liquid is input to and takes off the C5 tower, the described liquid of the liquid collected at the bottom of absorption agent tower tower and described secondary desorption tower bottom collecting that takes off converges by carrying out the absorption agent circulation from the input of top, absorption tower after the overcooling heat exchange, material in the described C5 of taking off tower separates through mass transfer, collect from the described C5 of taking off top of tower and obtain butylene, the bottom obtains C5 and reaches more heavy constituent, middle part lateral line withdrawal function butane, described absorption agent is that in molecule, carbonatoms is the alcohols of 1-4, at least a in ethers or ketone.The characteristics of the method be adopt carbonatoms be alcohols, ethers or the ketone of 1-4 as absorption agent, introduce outside system, and may be residual with the impurity form in product separation.
CN 101445419A discloses the separation method of the lower hydrocarbon containing light gas that a kind of rectifying combines with solvent absorbing, the method comprises the following steps: (1) will deliver to the precut tower after will being cooled to 10 ℃ to-37 ℃ through pretreated reactor outlet gas, this column overhead product comprises methane, hydrogen and other light gas, part carbon two and a small amount of carbon three that balances each other, and the tower reactor product is that all the other carbon two reach more heavy constituent; (2) precut tower exit gas is delivered to an absorption tower, separate wherein carbon one and carbon two with carbon three or carbon four or carbon five or carbon six or its hydrocarbon mixture as absorption agent, absorption tower tower top product comprises methane, hydrogen and other light gas and a small amount of carbon two and the absorption agent that balance each other, and the tower reactor product is the above component of carbon two and a small amount of hydrogen, methane; (3) bottom product on absorption tower is delivered to the precut tower, further absorbs C-2-fraction and removes methane and more deliver to the clear cutting that deethanizing column carries out carbon two and carbon three after light constituent at this tower; Deethanizer overhead obtains C-2-fraction, goes ethylene rectification tower to separate and obtains ethene and ethane, and the tower reactor product is that carbon three reaches more heavy constituent; Contain acetylene if enter in the charging of precut tower, the deethanizer overhead product first takes off acetylene and enters ethylene rectification tower again, is purified to needed mass concentration.The characteristics of CN 101445419A method are to adopt solvent absorption that precut column overhead product (comprising methane, hydrogen and other light gas, part carbon two and a small amount of carbon three that balances each other) is divided into carbon one and more light constituent and carbon two, carbon three components, what be that the method solves is the problem that carbon one separates with carbon two, and the method that how combines with solvent absorbing by rectifying obtains the problem of ethene.
Summary of the invention
For the problems of the prior art, the method that the present invention adopts oil to absorb, provide a kind of for to contain methane, carbon two, carbon three, carbon four and carbon five and more the catalytic cracking reaction gas product of heavy constituent effectively separate, not only energy-conservation but also can save facility investment, and can obtain separation system and the method for polymerization-grade propylene.
One of purpose of the present invention is to provide the system of a kind of absorption extraction catalytic pyrolysis gas product polymerization-grade propylene processed.Adopt predepropanization tower, debutanizing tower that the catalytic pyrolysis gas product is divided into carbon three and more light constituent, carbon four components and carbon five and more heavy constituent (raw pyrolysis gasoline), and with carbon four components or carbon five and more restructuring be divided into absorption agent, absorption tower and desorption tower to carbon three and more light constituent carry out absorption and desorption, be separated into carbon three and carbon two and light constituent more, more finally obtain the polymerization-grade propylene product through propylene tower.
Further, the system of absorption extraction catalytic pyrolysis gas product of the present invention polymerization-grade propylene processed comprises depropanizing tower, debutanizing tower and propylene tower.Wherein depropanizing tower comprises predepropanization tower and rear depropanizing tower; Be sequentially set with debutanizing tower, absorption tower, desorption tower between predepropanization tower and rear depropanizing tower, be provided with propylene tower after rear depropanizing tower; And be provided with the rich gas surge tank between absorption tower and desorption tower.
The catalytic pyrolysis gas product through the predepropanization tower be separated into carbon three and more light constituent reach more heavy constituent with carbon four; With carbon four and more heavy constituent separate through debutanizing tower and obtain carbon four components and carbon five and heavy constituent (raw pyrolysis gasoline) more, with carbon four components or carbon five and more heavy constituent as absorption agent in the absorption tower to the carbon three of predepropanization column overhead gas and more light constituent absorb, and by after the desorption tower desorb with carbon three components and carbon two and more light constituent separate; The desorption tower tower bottoms is delivered to rear depropanizing tower afterwards, and rear depropanizing tower overhead gas carries out the propane propylene separation through propylene tower, obtains the polymerization-grade propylene product in the propylene tower tower top.
The carbon three that the past depropanizing tower tower top comes reaches more, and light constituent enters the rich gas surge tank, after desorption tower overhead gas and absorption tower tower reactor liquid mix in the rich gas surge tank, the gas-liquid phase-splitting, gas phase enters the absorption tower tower reactor, liquid phase pump is delivered to the desorb tower top, and the desorption tower overhead gas is delivered to the rich gas surge tank.In this part flow process, heat exchange mode can be selected following three kinds: 1) the desorption tower overhead gas is entered the rich gas surge tank after water cooler is cooling, rich gas surge tank tank deck gas phase does not need the cooling absorption tower tower reactor that directly enters; 2) rich gas surge tank tank deck gas phase is entered the absorbing tower still after water cooler is cooling, and that the desorption tower overhead gas does not need is cooling, directly enters the rich gas surge tank; 3) namely with the cooling desorption tower overhead gas that enters the rich gas surge tank of water cooler, also simultaneously with the cooling rich gas surge tank head space gas that enters the absorption tower tower reactor of water cooler.Preferred front two kinds of heat exchange modes.
Before described predepropanization tower, by compressor, the catalytic cracking reaction gas product is compressed; Then lime set between gas phase and compressor section is delivered to the predepropanization tower.
Described rear depropanizing tower reactor liquid phase is after cooling, and a part is mixed with the absorption agent of debutanizing tower tower top or tower reactor as the circulation absorption agent, returns to the absorption tower; A part is sent outside as device product.
Described absorption tower top gaseous phase after condenser condenses, phlegma backflow absorption tower, the residue gas phase is sent out-of-bounds as the device byproduct.
The middle and upper part on described absorption tower can also arrange side cooler, and the self-absorption tower is drawn one material and return to the absorption tower after side cooler is cooling.Side cooler is set is conducive to strengthen absorption-desorption effect, can replace in addition absorbing the outer water cooler of tower top.
Particularly, system of the present invention is as follows:
The compressed machine compression of described catalytic pyrolysis gas product is delivered to the predepropanization tower with phlegma between gas phase and compressor section; And be separated into the carbon three of tower top and more carbon four and the heavy constituent more of light constituent and tower reactor through the predepropanization tower; Carbon four and more heavy constituent enter debutanizing tower and further be divided into carbon four components and carbon five and heavy constituent more;
During as absorption agent, carbon four components of debutanizing tower tower top obtain liquid phase carbon four components through condensation when carbon four components, and a part enters the absorption tower tower top as absorption agent, and a part is back to the debutanizing tower tower top, and the residue gas phase is delivered to catalytic cracking reaction device entrance; The carbon five of debutanizing tower tower bottoms and more heavy constituent is as the cooling rear discharge of raw pyrolysis gasoline out-of-bounds; When absorption agent is carbon five and more during heavy constituent, the carbon five of debutanizing tower tower reactor and more heavy constituent deliver to the absorption tower tower top after cooling; Carbon four components of debutanizing tower tower top obtain liquid phase carbon four components through condenser condenses, and a part drains into out-of-bounds, and a part is back to the debutanizing tower tower top; The residue gas phase is delivered to catalytic cracking reaction device entrance;
Be provided with the rich gas surge tank between absorption tower and desorption tower; In the past the carbon three that comes of depropanizing tower tower top and more light constituent enter the rich gas surge tank, after desorption tower overhead gas and absorption tower tower reactor liquid mix in the rich gas surge tank, the gas-liquid phase-splitting, gas phase enters the absorption tower tower reactor, liquid phase pump is delivered to the desorb tower top;
Enter the absorption agent of absorption tower tower top, contact with tower reactor rising gas phase, after absorbing carbon three components wherein, by the tower reactor extraction, with being pumped to the rich gas surge tank, absorption tower tower top extraction carbon two reaches more light constituent, after condenser condenses, phlegma backflow absorption tower, the residue gas phase is sent out-of-bounds as the device byproduct;
The carbon two of the carbon containing three of desorption tower overhead extraction and more the light constituent gas phase return to the rich gas surge tank, the tower reactor extraction contains the rich absorbent of carbon three components, more than being pumped in the middle part of rear depropanizing tower;
Rear depropanizing tower is separated into tower top gas carbon three and the poor absorption agent of tower bottoms with rich absorbent, and the cooling rear portion of tower bottoms is back to the absorption tower tower top as the circulation absorption agent, and a part is sent outside as device product; Rear depropanizing tower tower top gas carbon three components are delivered to propylene tower and are carried out the separation of propylene propane, obtain the polymerization-grade propylene product in the propylene tower tower top, and the propylene tower tower reactor obtains propane and discharges out-of-bounds.
In more detail, according to the difference of selected absorption agent, system of the present invention specifically describes as follows:
Carbon four components are as absorption agent: predepropanization tower top carbon three and more the light constituent gas phase be introduced into the rich gas surge tank, after cooled desorption tower top gas and absorption tower bottoms mix, the gas-liquid phase-splitting, gas phase enters the absorption tower tower reactor, with debutanizing tower tower top carbon four and after cooled depropanizing tower reactor liquid, as absorption agent, the carbon three in rich gas is absorbed; Liquid phase is with being pumped to the desorb tower top.Absorb top gaseous phase after condenser condenses, the residue gas phase is sent out-of-bounds as device byproduct dry gas.The desorb top gaseous phase is delivered to the rich gas surge tank after desorption tower top gas water cooler is cooling; The tower reactor liquid phase is by being pumped to rear depropanizing tower.Rear depropanizing tower top gaseous phase carbon three is delivered to propylene tower, carries out propylene propane and separates; Rear depropanizing tower reactor liquid phase is after cooling, and a part is mixed with debutanizing tower tower top carbon four as the circulation absorption agent, returns to the absorption tower; A part is sent outside as device product.Propylene tower tower top liquid-phase product is native system main products-polymerization-grade propylene, and the tower reactor product is propane.
Raw pyrolysis gasoline is as absorption agent: predepropanization tower top carbon three and more the light constituent gas phase be introduced into the rich gas surge tank, with the absorption tower bottoms and after mixing without cooling desorption tower overhead gas, the gas-liquid phase-splitting, gas phase enters the absorbing tower still after water cooler is cooling, with debutanizing tower tower reactor raw pyrolysis gasoline and after cooled depropanizing tower reactor liquid, as absorption agent, the carbon three in rich gas is absorbed; Liquid phase is with being pumped to the desorb tower top.Absorb top gaseous phase after condenser condenses, the residue gas phase is sent out-of-bounds as device byproduct dry gas.The desorb top gaseous phase is delivered to the rich gas surge tank; The tower reactor liquid phase is by being pumped to rear depropanizing tower.Rear depropanizing tower top gaseous phase carbon three is delivered to propylene tower, carries out propylene propane and separates; Rear depropanizing tower reactor liquid phase is after cooling, and a part is mixed with debutanizing tower tower reactor raw pyrolysis gasoline as the circulation absorption agent, returns to the absorption tower; A part is sent outside as device product.Propylene tower tower top liquid-phase product is this device main products-polymerization-grade propylene, and the tower reactor product is propane.
Above, the preferred version of system of the present invention is that carbon four components are as the system of absorption agent.
Above-described absorption agent can also partly or entirely adopt carbon four, carbon five, carbon six, carbon seven, carbon eight and the carbon nine introduced from described system outside to reach at least a in heavy constituent more.
When absorption agent was all introduced outside described system, carbon four components of debutanizing tower tower top obtained liquid phase carbon four components through condensation, and a part is back to the debutanizing tower tower top, and a part is sent out-of-bounds as product, and the residue gas phase is delivered to catalytic cracking reaction device entrance; The carbon five of debutanizing tower tower bottoms and more heavy constituent is as the cooling rear discharge of raw pyrolysis gasoline out-of-bounds.
Another object of the present invention is to provide the method for a kind of absorption extraction catalytic pyrolysis gas product polymerization-grade propylene processed.The principal feature of the inventive method is, adopt self-produced carbon four components of device or carbon five and more heavy constituent (raw pyrolysis gasoline) as absorption agent, the depropanizing tower top gas is absorbed, with wherein carbon three and carbon two and more light constituent is separately.
Particularly, according to the method that adopts the above system's absorption extraction catalytic pyrolysis gas product of the present invention polymerization-grade propylene processed, method of the present invention comprise separation of carbon three and more light constituent and carbon four and more heavy constituent, separation of carbon four components and carbon five and more heavy constituent, separation of carbon three components and carbon two reach more light constituent, reach separation of propylene and propane and make propylene; It is characterized in that: the catalytic pyrolysis gas product through the predepropanization tower be separated into carbon three and more light constituent reach more heavy constituent with carbon four; Reaching carbon four more, heavy constituent reaches more heavy constituent through carbon four components and the carbon five that the debutanizing tower separation obtains, with carbon four components or carbon five and more heavy constituent as absorption agent in the absorption tower to the carbon three of predepropanization column overhead gas and more light constituent absorb, and by after the desorption tower desorb with carbon three components and carbon two and more light constituent separate; The desorption tower tower bottoms is delivered to rear depropanizing tower afterwards, through after depropanizing tower separate, tower top gas carbon three components are carried out the propane propylene separation through propylene tower, obtain polymerization-grade propylene in the propylene tower tower top.
Wherein, in the past the carbon three that comes of depropanizing tower tower top and more light constituent mix in the rich gas surge tank with desorption tower overhead gas and absorption tower tower reactor liquid, gas-liquid phase-splitting after the rich gas balance, gas phase enters the absorption tower tower reactor, liquid phase pump is delivered to the desorb tower top, and the desorption tower overhead gas is delivered to the rich gas surge tank.
Preferably, method of the present invention, the compressed 1.0-2.1MPa that boosts to of wherein said catalytic cracking reaction gas product, and deliver to the predepropanization tower after being cooled to 36-60 ℃, between compressor section, lime set is pressurized to 1.0-2.1MPa with pump and delivers to the predepropanization tower;
Described predepropanization tower working pressure is 0.9-2.0MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 60-120 ℃;
Described debutanizing tower working pressure is 0.2-1.4MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 100-150 ℃;
Described absorption tower working pressure is 0.2-1.9MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 40-90 ℃;
Described rich gas surge tank working pressure is 0.2-1.9MPa, and service temperature is 40-95 ℃;
Described desorption tower working pressure is 0.2-1.9MPa, and tower top temperature is 40-95 ℃, and the tower reactor temperature is 100-150 ℃;
Described rear depropanizing tower working pressure is 0.9-2.5MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 100-150 ℃.
Described propylene tower working pressure is 1.0-2.5MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 40-90 ℃.
In addition, middle and upper part, described absorption tower can arrange side cooler, and the self-absorption tower is drawn one material and return to the absorption tower after side cooler is cooled to 36-60 ℃.
Described desorption tower overhead gas enters the rich gas surge tank after being cooled to 36-60 ℃, rich gas surge tank tank deck gas phase does not need the cooling absorption tower tower reactor that directly enters; Perhaps rich gas surge tank tank deck gas phase is entered the absorbing tower still after being cooled to 36-60 ℃, and that the desorption tower overhead gas does not need is cooling, directly enters the rich gas surge tank; Perhaps both the desorption tower overhead gas had been entered the rich gas surge tank after being cooled to 36-60 ℃, also simultaneously cooling rich gas surge tank head space gas enters the absorbing tower still after 36-60 ℃.Preferred following two kinds:
During as absorption agent, the desorption tower overhead gas enters described rich gas surge tank after being cooled to 36-60 ℃ when carbon four components; Rich gas surge tank tank deck gas phase is without the cooling absorption tower tower reactor that directly enters;
When absorption agent is carbon five and more during heavy constituent, the desorption tower overhead gas is without the cooling rich gas surge tank that directly enters; Rich gas surge tank tank deck gas phase enters the absorbing tower still after being cooled to 36-60 ℃.
When absorption agent is the carbon five of debutanizing tower tower reactor and more during heavy constituent, carbon five and more heavy constituent be cooled to 36-60 ℃ through water cooler and send into the absorption tower.
The poor absorption agent of rear depropanizing tower tower bottoms is after cooling, and a part is mixed with the absorption agent of debutanizing tower tower top or tower reactor, returns to the absorption tower as the circulation absorption agent; A part is sent outside as device product.Its cooling temperature is preferably to 36-60 ℃.Present method keeps the optimization right of logistics heat exchanger network flow process in adjustment System, and the waste heat of poor absorption agent can be used for and other logistics heat exchange, as poor absorption agent and catalytic cracking reaction charging heat exchange with recovery waste heat, thereby reach energy-saving and cost-reducing purpose.
Advantage and the beneficial effect of the system and method for a kind of absorption extraction catalytic pyrolysis gas product of the present invention polymerization-grade propylene processed are as follows:
1. reduction energy consumption
The present invention has reduced energy consumption from following several aspects: 1. the present invention has replaced with absorption tower, desorption tower and rear depropanizing tower the ethylene column that traditional separation method adopts, pass through operation conditions optimization, above-mentioned three column overhead service temperatures can be controlled in 36-60 ℃, can use recirculated cooling water to carry out cooling, condensation; And the ethylene column tower top temperature that traditional separation method adopts needs to adopt even propylene refrigerant condensation of refrigerated water below 0 ℃, so the inventive method can avoid using cryogenic coolant, greatly reduces energy consumption; 2. in the inventive method absorption tower, desorption tower and rear depropanizing tower working pressure between 0.2MPa-2.5MPa, the ethylene column working pressure that adopts than traditional separation method reduces greatly, and after Optimizing operation, can make predepropanization tower top working pressure greater than the absorption tower working pressure, therefore the predepropanization top gaseous phase just need not compress and can enter the absorption tower, thereby the decrease compression work reduces power consumption.
2. saving facility investment
1. because the inventive method can avoid using cryogenic coolant, therefore adopt the device of the inventive method that freezing unit can be set, thereby save a large amount of facility investments.2. in the inventive method, predepropanization tower top working pressure is greater than the absorption tower working pressure, the predepropanization top gaseous phase just need not compress can enter the absorption tower, therefore can avoid arranging special compressor or special compression section is set on the gas product compressor, thereby reduce the complicacy of compressor unit, reduce investment.3. the inventive method has replaced with absorption tower, desorption tower and rear depropanizing tower the ethylene column that traditional separation method adopts, and this three towers operational condition is gentle, can avoid using the special steel material of more expensive low temperature resistant, the high pressure of price, therefore can reduce the equipment and materials expense.
3. keep the higher propylene rate of recovery and purity
The inventive method, more than the rate of recovery of propylene can reach 98.5wt%, more than propylene product purity 99.5wt%, These parameters reached the level of traditional separation method, namely adopted the inventive method can not reduce product yield and purity.
System and method of the present invention can be applicable to Production of Propylene from C 4 Olefins by Catalytic Cracking (OCC) device, and similarly adopts the predepropanization separation process to produce the chemical plant installations of polymerization-grade propylene product.
Description of drawings
Below in conjunction with accompanying drawing, the present invention is described in further detail:
Fig. 1: prior art adopts the schematic flow sheet of traditional cryogenic rectification separation method of cryogenic coolant condensation.
Fig. 2: the present invention adopts carbon four components as the schematic flow sheet of absorption agent.
Fig. 3: the present invention adopts raw pyrolysis gasoline as the schematic flow sheet of absorption agent.
as Fig. 2 and/or shown in Figure 3, system of the present invention comprises following major equipment successively: compressor 1, catalytic pyrolysis gas product 1-1, compressor outlet gas phase 1-2, lime set 1-3 between compressor section, intersegmental lime set pump 2, predepropanization tower 3, debutanizing tower 4, debutanizing tower condenser 5, debutylize tower reactor liquid pump 6, the liquid cooling of debutylize tower reactor is device 7 but, rich gas surge tank 8, absorption tower 9, absorb overhead condenser 12, absorb tower reactor pump 11, desorb tower top water cooler 10a (Fig. 2), rich gas balance tank deck water cooler 10b (Fig. 3), desorption tower fresh feed pump 13, desorption tower 14, rear depropanizing tower fresh feed pump 15, rear depropanizing tower 16, the liquid cooling of rear depropanizing tower reactor is device 17 but, propylene tower 18.
Embodiment
Describe the present invention in detail in conjunction with above accompanying drawing and following embodiment, but interest field of the present invention is not limited by embodiment.
System and method of the present invention can adopt the general PRO II of chemical engineering technical field or ASPENPLUS simulation software to carry out simulation test to get analog reslt.
As shown in Figure 2, the compressed machine 1 of catalytic cracking reaction gas product is compressed to 1.5MPa, the outlet gas phase is cooled to 45 ℃ and the intersegmental lime set after intersegmental lime set pump 2 supercharging 1.5MPa and all delivers to predepropanization tower 3 middle and upper parts, and predepropanization tower 3 is separated into carbon three and more light constituent and carbon four and more heavy constituent with the catalytic cracking reaction gas product.Predepropanization tower 3 working pressures are 1.3MPa, and tower top temperature is 36 ℃, and the tower reactor temperature is about 90 ℃.The carbon four of predepropanization tower 3 tower reactors and more heavy constituent deliver to debutanizing tower 4 and be separated into carbon four components and carbon five and heavy constituent more.Described debutanizing tower working pressure is 0.8MPa, and tower top temperature is 57 ℃, and the tower reactor temperature is 122 ℃.Debutanizing tower 4 overhead gases are carbon four components, according to the different requirements of catalytic cracking reaction, part carbon four can be back to the catalytic cracking reaction unit with gas phase or liquid phase, to improve reaction conversion ratio; Liquid phase carbon four parts that debutanizing tower 4 overhead gas condensations are obtained are as trim the top of column, and a part of extraction is delivered to absorption tower 9 and made absorption agent.Debutanizing tower 4 tower reactor extraction carbon five reach more heavy constituent, are device byproduct-raw pyrolysis gasoline.The carbon three of predepropanization tower 3 tower tops and more the light constituent gas phase deliver to rich gas surge tank 8, after cooled desorption tower 14 overhead gases and absorption tower 9 tower bottomss mix, the gas-liquid phase-splitting, gas phase enters absorption tower 9 tower reactors.Rich gas surge tank working pressure is 1.1MPa, and service temperature is 52 ℃.In absorption tower 9 debutanizing tower 4 tower top carbon four components and through be cooled to after 45 ℃ after depropanizing tower 16 still liquid, as absorption agent, the carbon three in rich gas is absorbed; Absorption tower 9 working pressures are 1.0MPa, and tower top temperature is 36 ℃, and the tower reactor temperature is about 60 ℃.8 end of rich gas surge tank liquid phase is delivered to desorption tower 14 tower tops with desorption tower fresh feed pump 13, and desorption tower 14 working pressures are 1.2MPa, and tower top temperature is 45 ℃, and the tower reactor temperature is about 90 ℃.Absorption tower 9 top gaseous phases are after absorbing overhead condenser 12 condensations, and the residue gas phase is sent out-of-bounds as device byproduct dry gas.Desorption tower 14 top gaseous phases are delivered to rich gas surge tank 8 after desorption tower top gas water cooler 10a is cooled to 45 ℃; Desorption tower 14 tower reactor liquid phases are delivered to rear depropanizing tower 16 by rear depropanizing tower fresh feed pump 15; Rear depropanizing tower working pressure is 1.9MPa, and tower top temperature is 45 ℃, and the tower reactor temperature is about 110 ℃.Rear depropanizing tower 16 top gaseous phase carbon three components are delivered to propylene tower 18, carry out propylene propane and separate; Rear depropanizing tower 16 still liquid phases through after depropanizing tower reactor liquid cooling but after cooling 45 ℃ of device 17, a part is mixed with debutanizing tower 4 tower top carbon four as the circulation absorption agent, returns to absorption tower 9; A part is sent outside as device product.Propylene tower 18 tower top liquid-phase products are native system main products-polymerization-grade propylene, and the tower reactor product is propane.The propylene tower working pressure is 1.8MPa, and tower top temperature is 42 ℃, and the tower reactor temperature is about 54 ℃.
As shown in Figure 3, the compressed machine 1 of catalytic cracking reaction gas product is compressed to 1.5MPa, the outlet gas phase is cooled to 45 ℃ and the intersegmental lime set after intersegmental lime set pump 2 is pressurized to 1.5MPa and all delivers to predepropanization tower 3 middle and upper parts, and predepropanization tower 3 is divided into carbon three and more light constituent and carbon four and more heavy constituent with the catalytic cracking reaction gas product.Predepropanization tower 3 working pressures are 1.3MPa, and tower top temperature is 36 ℃, and the tower reactor temperature is about 90 ℃.Predepropanization tower 3 tower reactor carbon four and more heavy constituent deliver to debutanizing tower 4 and be separated into carbon four components and carbon five and heavy constituent more.Described debutanizing tower working pressure is 0.8MPa, and tower top temperature is 57 ℃, and the tower reactor temperature is 122 ℃.Debutanizing tower 4 overhead gases are carbon four components, different requirements according to catalytic cracking reaction, part carbon four can be back to reaction member with gas phase or liquid phase, to improve reaction conversion ratio, as trim the top of column, a part is as the extraction of device byproduct with liquid phase carbon four parts of debutanizing tower 4 overhead gas condensations.Debutanizing tower 4 tower reactor extraction carbon five reach more heavy constituent, after interchanger 7 is cooled to 45 ℃, deliver to absorption tower 9 tower tops as absorption agent.Predepropanization tower 3 tower top carbon three and more the light constituent gas phase deliver to rich gas surge tank 8, after desorption tower 14 overhead gases and absorption tower 9 still liquid mix, the gas-liquid phase-splitting, gas phase enters absorption tower 9 tower reactors after rich gas balance tank deck water cooler 10b is cooled to 45 ℃.Rich gas surge tank working pressure is 1.1MPa, and service temperature is 55 ℃.Debutanizing tower 4 tower reactor raw pyrolysis gasolines cooling after and through be cooled to after 45 ℃ after depropanizing tower 16 still liquid, as absorption agent, the carbon three in rich gas is absorbed; Absorption tower 9 working pressures are 1.0MPa, and tower top temperature is 36 ℃, and the tower reactor temperature is about 60 ℃.At the bottom of rich gas surge tank 8 tanks, liquid phase is delivered to desorption tower 14 tower tops with desorption tower fresh feed pump 13; Desorption tower 14 working pressures are 1.2MPa, and tower top temperature is 45 ℃, and the tower reactor temperature is about 90 ℃.Absorption tower 9 top gaseous phases are after absorbing overhead condenser 12 condensations, and the residue gas phase is sent out-of-bounds as device byproduct dry gas.Desorption tower 14 top gaseous phases are delivered to rich gas surge tank 8; Desorption tower 14 tower reactor liquid phases are delivered to rear depropanizing tower 16 by rear depropanizing tower fresh feed pump 15; Rear depropanizing tower working pressure is 1.9MPa, and tower top temperature is 45 ℃, and the tower reactor temperature is about 110 ℃.Rear depropanizing tower 16 top gaseous phase carbon three are delivered to propylene tower 18, carry out propylene propane and separate; Rear depropanizing tower 16 still liquid phases through after depropanizing tower reactor liquid cooling but after cooling 45 ℃ of device 17, a part is mixed with debutanizing tower 4 tower reactor raw pyrolysis gasolines as the circulation absorption agent, returns to absorption tower 9; A part is sent outside as device product.Propylene tower 18 tower top liquid-phase products are this device main products-polymerization-grade propylene, and the tower reactor product is propane.The propylene tower working pressure is 1.8MPa, and tower top temperature is 42 ℃, and the tower reactor temperature is about 54 ℃.
Comparison diagram 2, two kinds of flow processs shown in Figure 3, except the difference that causes because of absorption agent difference used, the cooling process of rich gas that enters absorption tower 9 is also different, a kind of is that desorption tower 14 overhead gases enter rich gas surge tank 8 after cooling, mix with predepropanization tower 3 overhead gases, after the gas-liquid phase-splitting, gas phase is no longer cooling, directly enters absorption tower 9 tower reactors; A kind of is the not cooling rich gas surge tanks 8 that directly enter of desorption tower 14 overhead gases, mixes with predepropanization tower 3 overhead gases, and after the gas-liquid phase-splitting, gas phase after water cooler 10 is cooling, enters absorption tower 9 tower reactors again.These two kinds of method of cooling absorb flow process for carbon four and raw pyrolysis gasoline absorption flow process is all applicable, and can use simultaneously.But preferred Fig. 2 and heat exchange process shown in Figure 3.
The industrial implementation example:
The catalytic cracking reaction gas product classical group of producing Production of Propylene from C 4 Olefins by Catalytic Cracking (OCC) device of 80,000 tons of propylene per year becomes to see Table one.
Table one OCC catalytic cracking reaction gas product forms
Its catalytic cracking reaction gas product flow is 74733.3kg/hr.
The present embodiment adopts carbon four components as shown in Figure 2 to do the system and method for absorption agent flow process, adopts PRO II simulation software to carry out simulation test, obtains analog reslt as shown in Table 2.
By result shown in table two as can be known:
1. reduction energy consumption
Absorption tower, desorption tower and rear depropanizing tower service temperature are controlled at 36-60 ℃, can use recirculated cooling water to carry out cooling, condensation, need not to adopt cryogenic coolant, and be capable of reducing energy consumption; Absorption tower, desorption tower and rear depropanizing tower working pressure are between 0.2MPa-2.5MPa, the ethylene column working pressure that adopts than traditional separation method reduces greatly, and after Optimizing operation, can make predepropanization tower top working pressure greater than the absorption tower working pressure, therefore the predepropanization top gaseous phase just need not compress and can enter the absorption tower, thereby the decrease compression work reduces power consumption.
2. saving facility investment
1. adopt the inventive method that freezing unit needn't be set, thereby save a large amount of facility investments.2. in the inventive method, predepropanization tower top working pressure is greater than the absorption tower working pressure, the predepropanization top gaseous phase just need not compress can enter the absorption tower, therefore can avoid arranging special compressor or special compression section is set on the gas product compressor, thereby reduce the complicacy of compressor unit, reduce investment.3. the inventive method has replaced with absorption tower, desorption tower and rear depropanizing tower the ethylene column that traditional separation method adopts, and this three towers operational condition is gentle, can avoid using the special steel material of more expensive low temperature resistant, the high pressure of price, therefore can reduce the equipment and materials expense.
3. keep the higher propylene rate of recovery and purity
The inventive method, more than the rate of recovery of propylene can reach 98.5wt%, more than propylene product purity 99.5wt%, These parameters reached the level of traditional separation method, namely adopted the inventive method can not reduce product yield and purity.
Claims (15)
1. the system of an absorption extraction catalytic pyrolysis gas product polymerization-grade propylene processed, comprise depropanizing tower, debutanizing tower and propylene tower; It is characterized in that:
Depropanizing tower comprises predepropanization tower and rear depropanizing tower; Be sequentially set with debutanizing tower, absorption tower, desorption tower between predepropanization tower and rear depropanizing tower, be provided with propylene tower after rear depropanizing tower; And be provided with the rich gas surge tank between absorption tower and desorption tower;
The catalytic pyrolysis gas product through the predepropanization tower be separated into carbon three and more light constituent reach more heavy constituent with carbon four; With carbon four and more heavy constituent separate through debutanizing tower and obtain carbon four components and carbon five and heavy constituent more, with carbon four components or carbon five and more heavy constituent as absorption agent in the absorption tower to the carbon three of predepropanization column overhead gas and more light constituent absorb, and by after the desorption tower desorb with carbon three components and carbon two and more light constituent separate; Wherein in the past the carbon three that comes of depropanizing tower tower top and more light constituent enter the rich gas surge tank, after desorption tower overhead gas and absorption tower tower reactor liquid mix in the rich gas surge tank, the gas-liquid phase-splitting, gas phase enters the absorption tower tower reactor, liquid phase pump is delivered to the desorb tower top; The desorption tower overhead gas is delivered to the rich gas surge tank, and the desorption tower tower bottoms is delivered to rear depropanizing tower, and rear depropanizing tower overhead gas carries out the propane propylene separation through propylene tower, obtains the polymerization-grade propylene product in the propylene tower tower top.
2. the system as claimed in claim 1 is characterized in that:
Described rear depropanizing tower reactor liquid phase is after cooling, and a part is mixed with the absorption agent of debutanizing tower tower top or tower reactor as the circulation absorption agent, returns to the absorption tower; A part is sent outside as device product.
3. the system as claimed in claim 1 is characterized in that:
Described absorption tower top gaseous phase after condenser condenses, phlegma backflow absorption tower, the residue gas phase is sent out-of-bounds as the device byproduct.
4. the system as claimed in claim 1 is characterized in that:
Middle and upper part, described absorption tower arranges intermediate condenser, and the self-absorption tower is drawn one material and return to the absorption tower after side cooler is cooling.
5. the system as claimed in claim 1 is characterized in that:
When absorption agent was carbon four component, carbon four components of debutanizing tower tower top obtained liquid phase carbon four components through condensation, and a part enters the absorption tower tower top as absorption agent, and a part is back to the debutanizing tower tower top, and the residue gas phase is delivered to catalytic cracking reaction device entrance; The carbon five of debutanizing tower tower bottoms and more heavy constituent is as the cooling rear discharge of raw pyrolysis gasoline out-of-bounds;
When absorption agent is carbon five and more during heavy constituent, the carbon five of debutanizing tower tower reactor and more heavy constituent deliver to the absorption tower tower top after cooling; Carbon four components of debutanizing tower tower top obtain liquid phase carbon four components through condenser condenses, and a part drains into out-of-bounds, and a part is back to the debutanizing tower tower top; The residue gas phase is delivered to catalytic cracking reaction device entrance.
6. the system as claimed in claim 1 is characterized in that:
The carbon three that the past depropanizing tower tower top comes reaches more, and light constituent enters the rich gas surge tank, after cooled desorption tower overhead gas and absorption tower tower reactor liquid mix in the rich gas surge tank, the gas-liquid phase-splitting, gas phase is without the cooling absorption tower tower reactor that directly enters, and liquid phase pump is delivered to the desorb tower top;
Perhaps, in the past the carbon three that comes of depropanizing tower tower top and more light constituent enter the rich gas surge tank, with absorption tower tower reactor liquid and after mixing in the rich gas surge tank without cooling desorption tower overhead gas, the gas-liquid phase-splitting, gas phase enters the absorbing tower still after cooling, liquid phase pump is delivered to the desorb tower top.
7. the system as claimed in claim 1 is characterized in that:
Before described predepropanization tower, by compressor, the catalytic cracking reaction gas product is compressed; Then lime set between gas phase and compressor section is delivered to the predepropanization tower.
8. the system as claimed in claim 1 is characterized in that:
Described absorption agent partly or entirely adopts carbon four, carbon five, carbon six, carbon seven, carbon eight and the carbon nine introduced from described system outside to reach at least a in heavy constituent more;
When absorption agent is all introduced outside described system, carbon four components of debutanizing tower tower top obtain liquid phase carbon four components through condensation, a part is back to the debutanizing tower tower top, and a part is sent out-of-bounds as system's byproduct, and the residue gas phase is delivered to catalytic cracking reaction device entrance; Debutanizing tower tower reactor liquid phase carbon five and more heavy constituent send out-of-bounds after cooling as raw pyrolysis gasoline.
9. system as described in any one of claim 1～8 is characterized in that comprising:
Compressor, predepropanization tower, debutanizing tower, absorption tower system, rich gas surge tank, desorption tower, rear depropanizing tower, propylene tower;
The compressed machine compression of described catalytic pyrolysis gas product is delivered to the predepropanization tower with phlegma between gas phase and compressor section; And be separated into the carbon three of tower top and more carbon four and the heavy constituent more of light constituent and tower reactor through the predepropanization tower; Carbon four and more heavy constituent enter debutanizing tower and further be separated into carbon four components and carbon five and heavy constituent more;
During as absorption agent, carbon four components of debutanizing tower tower top obtain liquid phase carbon four components through condensation when carbon four components, and a part enters the absorption tower tower top as absorption agent, and a part is back to the debutanizing tower tower top, and the residue gas phase is delivered to catalytic cracking reaction device entrance; The carbon five of debutanizing tower tower bottoms and more heavy constituent is as the cooling rear discharge of raw pyrolysis gasoline out-of-bounds; Be provided with the rich gas surge tank between absorption tower and desorption tower, the carbon three that the past depropanizing tower tower top comes reaches more, and light constituent enters the rich gas surge tank, after cooled desorption tower overhead gas and absorption tower tower reactor liquid mix in the rich gas surge tank, the gas-liquid phase-splitting, gas phase is without the cooling absorption tower tower reactor that directly enters, and liquid phase pump is delivered to the desorb tower top;
When absorption agent is carbon five and more during heavy constituent, the carbon five of debutanizing tower tower reactor and more heavy constituent deliver to the absorption tower tower top after cooling; Carbon four components of debutanizing tower tower top obtain liquid phase carbon four components through condenser condenses, and a part drains into out-of-bounds, and a part is back to the debutanizing tower tower top; The residue gas phase is delivered to catalytic cracking reaction device entrance; Be provided with the rich gas surge tank between absorption tower and desorption tower, the carbon three that the past depropanizing tower tower top comes reaches more, and light constituent enters the rich gas surge tank, with absorption tower tower reactor liquid and after mixing in the rich gas surge tank without cooling desorption tower overhead gas, the gas-liquid phase-splitting, gas phase enters the absorbing tower still after cooling, liquid phase pump is delivered to the desorb tower top;
Enter the absorption agent of absorption tower tower top, contact with tower reactor rising gas phase, after absorbing carbon three components wherein, by the tower reactor extraction, with being pumped to the rich gas surge tank, absorption tower tower top extraction carbon two reaches more light constituent, after condenser condenses, phlegma backflow absorption tower, the residue gas phase is sent out-of-bounds as the device byproduct; The absorption tower arranges intermediate condenser, and the self-absorption tower is drawn one material and return to the absorption tower after side cooler is cooling;
Desorption tower overhead extraction gas phase is returned to the rich gas surge tank, and the tower reactor extraction contains the rich absorbent of carbon three components, more than being pumped to rear depropanizing tower middle part;
Rear depropanizing tower is separated into tower top gas carbon three and the poor absorption agent of tower bottoms with rich absorbent, and the cooling rear portion of tower bottoms is back to the absorption tower tower top as the circulation absorption agent, and a part is sent outside as device product; Rear depropanizing tower tower top gas carbon three components are delivered to propylene tower and are carried out the separation of propylene propane, obtain the polymerization-grade propylene product in the propylene tower tower top, and the propylene tower tower reactor obtains propane and discharges out-of-bounds.
10. adopt the method for according to claim 1～9 any one described system absorption extraction catalytic pyrolysis gas product polymerization-grade propylene processed, comprise separation of carbon three and more light constituent and carbon four and more heavy constituent, separation of carbon four components and carbon five and more heavy constituent, separation of carbon three components and carbon two reach more light constituent, reach separation of propylene and propane and make polymerization-grade propylene; It is characterized in that:
The catalytic pyrolysis gas product through the predepropanization tower be separated into carbon three and more light constituent reach more heavy constituent with carbon four; With carbon four and more heavy constituent separate through debutanizing tower and obtain carbon four components and carbon five and heavy constituent more, with carbon four components or carbon five and more heavy constituent as absorption agent in the absorption tower to the carbon three of predepropanization column overhead gas and more light constituent absorb, and by after the desorption tower desorb with carbon three components and carbon two and more light constituent separate; Wherein in the past the carbon three that comes of depropanizing tower tower top and more light constituent mix in the rich gas surge tank with desorption tower overhead gas and absorption tower tower reactor liquid, gas-liquid phase-splitting after the rich gas balance, gas phase enters the absorption tower tower reactor, and liquid phase pump is delivered to the desorb tower top, and the desorption tower overhead gas is delivered to the rich gas surge tank; The desorption tower tower bottoms is delivered to rear depropanizing tower afterwards, through after depropanizing tower separate, tower top gas carbon three components are carried out the propane propylene separation through propylene tower, obtain polymerization-grade propylene in the propylene tower tower top.
11. method as claimed in claim 10 is characterized in that:
The compressed 1.0-2.1MPa that boosts to of described catalytic cracking reaction gas product, and deliver to the predepropanization tower after being cooled to 36-60 ℃, between compressor section, lime set is pressurized to 1.0-2.1MPa with pump and delivers to the predepropanization tower;
Described predepropanization tower working pressure is 0.9-2.0MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 60-120 ℃;
Described debutanizing tower working pressure is 0.2-1.4MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 100-150 ℃;
Described absorption tower working pressure is 0.2-1.9MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 40-90 ℃;
Described rich gas surge tank working pressure is 0.2-1.9MPa, and service temperature is 40-95 ℃;
Described desorption tower working pressure is 0.2-1.9MPa, and tower top temperature is 40-95 ℃, and the tower reactor temperature is 100-150 ℃;
Described rear depropanizing tower working pressure is 0.9-2.5MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 100-150 ℃;
Described propylene tower working pressure is 1.0-2.5MPa, and tower top temperature is 36-60 ℃, and the tower reactor temperature is 40-90 ℃.
12. method as claimed in claim 11 is characterized in that:
Draw one material from described absorption tower and return to the absorption tower after side cooler is cooled to 36-60 ℃.
13. method as claimed in claim 11 is characterized in that:
The desorption tower overhead gas enters described rich gas surge tank after being cooled to 36-60 ℃; Rich gas surge tank tank deck gas phase is without the cooling absorption tower tower reactor that directly enters;
Perhaps, the desorption tower overhead gas is without the cooling rich gas surge tank that directly enters; Rich gas surge tank tank deck gas phase enters the absorbing tower still after being cooled to 36-60 ℃.
14. the separation method of acquisition polymerization-grade propylene as claimed in claim 11 is characterized in that:
When absorption agent is the carbon five of debutanizing tower tower reactor and more during heavy constituent, carbon five and more heavy constituent be cooled to 36-60 ℃ through water cooler and send into the absorption tower.
15. the separation method of acquisition polymerization-grade propylene as claimed in claim 11 is characterized in that:
The poor absorption agent of described rear depropanizing tower tower reactor is cooled to 36-60 ℃ through interchanger, and a part is mixed with the absorption agent of debutanizing tower tower top or tower reactor, returns to the absorption tower as the circulation absorption agent; A part is sent outside as device product.
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