CN103012033A - Method for separating propylene and propane from liquid hydrocarbon - Google Patents
Method for separating propylene and propane from liquid hydrocarbon Download PDFInfo
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- CN103012033A CN103012033A CN2011102844307A CN201110284430A CN103012033A CN 103012033 A CN103012033 A CN 103012033A CN 2011102844307 A CN2011102844307 A CN 2011102844307A CN 201110284430 A CN201110284430 A CN 201110284430A CN 103012033 A CN103012033 A CN 103012033A
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Abstract
The invention provides a method for separating propylene and propane from a liquid hydrocarbon. The method comprises the following steps of 1, determining if a mole content ratio of light components comprising C2 to propylene in a liquid hydrocarbon is less than 0.004 or not, and 2, if the mole content ratio is less than 0.004, separating propylene and propane having qualified quality from the liquid hydrocarbon by a twin-tower gas fractionation device mainly composed of a propane removal tower and a propylene rectifying tower. Through analysis of operation conditions of the traditional gas fractionation device and real data of composition of an upstream produced liquid hydrocarbon, the invention provides a novel simplified gas fractionation process. Compared with the traditional gas fractionation process, the novel simplified process has a high propylene yield, a short process, a low equipment cost, a low operation cost, and good economic benefits. The conversion of the traditional gas fractionation process and the novel simplified process is convenient. A liquid hydrocarbon satisfying the novel simplified process requirements can be obtained easily and has good applicability. The novel simplified process can be industrialized and popularized easily.
Description
Technical field
The invention belongs to the liquid hydrocarbon isolation technique, be specifically related to a kind of in liquid hydrocarbon the method for separation of propylene and propane.
Background technology
In recent years, the fast development of propenyl petroleum chemicals has greatly promoted increasing substantially of propylene consumption, and China's propone output far can not need by satisfying the market, and the propylene import volume accounts for 41% of propylene consumption.Propylene mainly comes from hydrocarbon steam cracking and catalytic cracking process, but along with the continuous minimizing of light crude reserves, output, hydrocarbon cracking technique ratio in production of propylene continues to reduce.Produce the propylene that reclaims in the liquid hydrocarbon by gas fractionation plant (gas separation unit) by catalytic cracking unit in 2008 and account for 26.8% of commodity propone output.Raising catalytic cracking cracking severity, raising liquid hydrocarbon productivity and propylene content thereof, improvement gas separation unit separating effect become one of effective way of propylene enhancing.
Traditional gas separation unit mainly is made of depropanizing tower, deethanizing column and propylene rectification tower three towers.Be the specification of quality (χ 〉=99.6%) that satisfies the polymerization-grade high-purity propylene, need establish the deethanizing column contained C that will liquefy
2 -Part removes.The restriction that is balanced each other, the deethanizing top gaseous phase is carried part propylene, propane inevitably secretly, causes propylene, propane yield not high.
Specifically can be obtained by three-column process flow analog result and propylene loss analysis:
1, basic data
In the PRO/II flowsheeting software, SRK state equation form is simple, accuracy is higher, can be used for simultaneously the vapour-liquid two-phase of nonpolar system and balance each other, enthalpy difference calculating etc.In this simulation process, the parameter that balances each other, enthalpy and density of gas phase adopt the SRK state equation, and the normal equation in the PRO/II flowsheeting software is adopted in the calculating of all the other physical property.
1.1 liquid hydrocarbon forms
The liquid hydrocarbon that data come from domestic different petroleum chemical enterprises gas separation unit forms, and the liquid hydrocarbon composition differs greatly, and specifically sees Table 1.The board design scale is by 2.0 * 10
4The t/a meter.
Table 1 gas separation unit liquid hydrocarbon forms (χ %)
| Form | Liquid hydrocarbon 1 | Liquid |
Liquid |
Liquid hydrocarbon 4 |
| C 2 - | 0.82 | 1.00 | 1.28 | 2.88 |
| C 3 ＝ | 43.88 | 35.45 | 42.93 | 43.02 |
| C 3 0 | 8.52 | 12.11 | 7.61 | 17.12 |
| i-C 4 0 | 15.98 | 16.92 | 14.30 | 19.42 |
| n-C 4 0 | 3.69 | 3.31 | 2.82 | 1.86 |
| C 4 ＝-1 | 5.22 | 5.65 | - | 8.51 |
| i-C 4 ＝ | 9.85 | 11.96 | 14.96 | - |
| t-C 4 ＝-2 | 5.17 | 4.93 | 4.99 | 3.23 |
| c-C 4 ＝-2 | 6.50 | 7.11 | 6.82 | 3.91 |
| C 5 + | 0.37 | 1.56 | 2.57 | 0.05 |
1.2 process stipulation
Depropanizing tower: tower reactor C
3≤ 1% (χ), cat head C
4≤ 0.5% (χ);
Deethanizing column: tower reactor C
2 -≤ 0.01% (χ);
Propylene tower (propylene distillation tower): cat head propylene product purity 〉=99.6% (χ), tower reactor propane product purity 〉=97.0% (χ).
1.3 operational condition
Each tower operational condition of table 2
Temperature distribution to some extent fluctuation with the variation of feed composition in the tower, refluxes that when overhead condenser, tower reactor reboiler also should be adjusted to some extent at each tower feed entrance point.
2, simulation process explanation (take liquid hydrocarbon 1 as example)
2.1 best feed entrance point
Each tower adopts PRO/II optimiser module to be optimized, and each a tower reflux ratio hour corresponding feed plate position is optimum feed entrance point.
2.2 working pressure
Take table 2 working pressure as reference, tower top pressure is subjected to the restriction of condenser low-temperature receiver (such as air, water) temperature, generally selects to be advisable about 45 ℃.
2.3T1 process stipulation
The main purpose of depropanizing tower is to remove C
4Above component, its cat head C
4Foreign matter content is larger on the impact of propylene tower propane quality product.By material balance, for production purity reaches propane product more than 97%, T1 cat head C
4Content is defined as 0.4% (χ).As shown in table 3, along with the T1 overhead stream is C in the T3 charging
4Deng the rising of foreign matter content, restructuring minute increase is conducive to the separation of propylene, propane in the propylene tower charging, the easier cat head that is evaporated to of propylene, and the overhead condenser load increases; The impact of being recombinated simultaneously minute and to increase is to guarantee the tower reactor quality product, and needing to increase reboiler could steam the propylene that affect purified propylene oxide, but works as T1 cat head C
4When content is 0.5%, obtain qualified propane product even propylene distillation tower tower reactor propylene all steamed also can not separate.
Table 3
| T1 cat head C 4Content (χ) | 0.3％ | 0.4％ | 0.5％ |
| The T3 reflux ratio | 16.86 | 17.00 | 22.62 |
| The T3 condenser duty/(Gcal/h) | -11.39 | -11.48 | -14.14 |
| The T3 reboiler/(Gcal/h) | 11.23 | 11.32 | 13.85 |
| T3 top pronane flow/(kmol/h) | 0.8327 | 0.8322 | 0.8061 |
| T3 tower reactor C 3 ＝Flow (kmol/h) | 0.4572 | 0.1874 | 0.0113 |
3, analog result and propylene loss analysis
The results are shown in Table 4, main propylene, propane yield and the loss distribution of different liquid hydrocarbons under the aforesaid operations condition of investigating in the three-column process flow simulation process.By table 3 analog result as can be known, along with C in the liquid hydrocarbon
2 -The increase of content, propylene, propane yield are on a declining curve, are not difficult to find out by table 4, and propene yield changes comparatively obvious, is followed successively by 96.01%, 94.31%, 94.37%, 90.03%, and the propane yield is followed successively by 94.26%, 94.33%, 93.56%, 93.52%.
Distribution situation by table 5, table 6 loss propylene, propane knows that the deethanizing cat head is the main position of propylene loss.Light constituent gathers at cat head, and for keeping pressure-stabilisation, the density of propylene that carries of speeding to exit accounts for the propylene total losses more than 80% up to more than 50%; Carry simultaneously 7%～8% propane secretly, the propane yield is also had certain impact.Propylene, propane losses amount are with liquid hydrocarbon C
2 -The increase of content and increasing.Because upstream device---light constituent content is defined as ∑ (C in the absorption-stabilization system by catalytic cracking liquid towards hydrocarbon
1+ C
2)≤3% χ), enter behind the gas separation unit and must just can obtain polymerization-grade propylene by the deethanizing operation, it is inevitable to cause that by the deethanizing operation propylene is carried phenomenon secretly.Domestic device propene yield is the highest only to be reached about 95%, and the propane yield is generally about 94%, behind process parameter optimizing yield also difficulty be significantly improved.
Several gas separation unit analog results of table 4
Table 5 propylene loss distributes
Table 6 propane losses distributes
Summary of the invention
The objective of the invention is to absorb based on gas fractionation plant liquid hydrocarbon production process one Optimizing operation of stabilization element, suitably reduce C in the liquid hydrocarbon
2Following light constituent concentration greatly reduces deethanizing column non-condensable gas amount; Might make the logistics of depropanizing cat head not need directly to advance propylene rectification tower and can obtain qualified propylene, propane product through the deethanizing operation, reduce to greatest extent propylene loss.
For this reason, technical scheme of the present invention is: a kind of method of in liquid hydrocarbon, isolating propylene and propane, and the method may further comprise the steps:
1) measures the C that comprises in the liquid hydrocarbon
2Whether compare less than 0.004 in interior light constituent and propylene molar content, if so, then carry out step 2);
2) double tower gas fractionator by mainly being comprised of depropanizing tower and propylene rectification tower is isolated high-purity propylene and qualified propane in above-mentioned liquid hydrocarbon; The formation of described double tower gas fractionator is that the opening for feed of depropanizing tower extracts raw material by liquid hydrocarbon pump from the liquid hydrocarbon tank, its top is provided with the first condenser, the first return tank and the first reflux pump, make the gas phase at its top after the first condenser condenses, be back to the first return tank, by the first reflux pump a condensation liquid phase part is sent into again rectifying of depropanizing tower afterwards, another part is squeezed into the propylene rectification tower opening for feed;
Depropanizing tower bottom is provided with reflux pump at the bottom of reboiler and the first tower, be back in the depropanizing tower after the first reboiler is heated to certain temperature so that depropanizing tower tower reactor liquid phase is delivered to through a reflux pump part at the bottom of the first tower, another part is as mixed c 4 output of products device; It is for rectifying tower provides thermal source that reboiler one is set at the bottom of the tower, the 2nd, and C at the bottom of the control tower
3Balanced contents is avoided carrying excessive C at the bottom of the tower
3Affect propylene, propane product yield as the output of the mixed c 4 of cheapness;
Described propylene rectification tower structure and depropanizing tower are similar, its top is provided with the second condenser, the second return tank and the second reflux pump, top gaseous phase is back to the second return tank through the second condenser condenses, is back in the propylene rectification tower by the second reflux pump afterwards, and another part is as output of products;
Propylene rectification tower bottom is provided with reflux pump at the bottom of the second reboiler and the second tower, so that propylene rectification tower tower reactor part liquid phase is back in the propylene rectification tower after reflux pump is delivered to the second reboiler at the bottom of the second tower, another part is as output of products;
In step 1) in measure in the liquid hydrocarbon and comprise C
2Whether compare less than 0.003 in interior light constituent and propylene molar content.
In step 1) in measure in the liquid hydrocarbon and comprise C
2Whether compare less than 0.0024 in interior light constituent and propylene molar content.
In the sepn process, by regulating C in the discharging of reflux ratio restriction depropanizing tower cat head
4Content is to guarantee the rectifying tower quality product, quantity of reflux restriction depropanizing tower tower reactor C at the bottom of the control tower
3Content is to guarantee the propylene tower product yield.
Advantage applies of the present invention is in the following aspects:
1, simplifies traditional three-column process flow (depropanizing tower, deethanizing column and propylene rectification tower), reduced cost of equipment and process cost;
2, propene yield, economic benefits have been improved;
3, the liquid hydrocarbon that satisfies the new technological process requirement is easy to get, has good suitability, and new and old flow process conversion is convenient, is easy to promote.
Description of drawings
Fig. 1 is the double tower gas fractionator schematic flow sheet.
Fig. 2 is different C
2 -/ C
3 =(χ) two tower reflux ratios, energy consumption figure under the liquid hydrocarbon.
Fig. 3 is different C
2 -/ C
3 =(χ) T3 reflux ratio, propene yield figure under the liquid hydrocarbon.
Fig. 4 is different C
3 =/ C
3 0(χ) T3 reflux ratio, propene yield figure under the liquid hydrocarbon.
Fig. 5 is different C
2 -/ C
3 =(χ) two kinds of maximum gas phase molar flow rate contrasts of flow process T3 under the liquid hydrocarbon.
The different C of Fig. 6
2 -/ C
3 =Two kinds of flow process T3 energy consumption comparison figure under the liquid hydrocarbon.
Embodiment
Technical scheme of the present invention is based on following two aspect technological thoughts and proposes:
1, because existing gas separation unit mainly is made of depropanizing tower, deethanizing column and propylene rectification tower three towers, for the specification of quality (χ 〉=99.6%) that satisfies the polymerization-grade high-purity propylene, need establish the deethanizing column C that liquid hydrocarbon is contained
2 -Part removes, yet, the restriction that is balanced each other, the deethanizing top gaseous phase is carried part propylene, propane inevitably secretly, cause propylene, propane yield not high, in order further to improve propylene, propane yield, the Optimizing operation by gas separation unit liquid hydrocarbon production process-absorption stabilization element has been proposed, suitably reduce C
2 -Concentration just can make deethanizing column non-condensable gas amount greatly reduce, and might make the logistics of depropanizing cat head not need directly to advance propylene rectification tower and can obtain qualified propylene product through the deethanizing operation, significantly reduces the loss of propylene.
2, in recent years, domestic catalytic cracking unit is by Optimizing operation, on the basis of improving liquid hydrocarbon yield, and C in the liquid hydrocarbon
2 -Concentration continues to reduce, for the double tower gas division technique of cancelling deethanizing column provides the liquid hydrocarbon basis.
Based on above-mentioned thought, present embodiment provides a kind of method of isolating propylene and propane in liquid hydrocarbon, and the method may further comprise the steps:
1) measures the C that comprises in the liquid hydrocarbon
2Whether less than 0.004, if so, then carry out step 2 at the ratio of interior light constituent molar content and propylene molar content);
2) double tower gas fractionator by mainly being comprised of depropanizing tower and propylene distillation tower is isolated propylene and propane in above-mentioned liquid hydrocarbon;
Wherein, consisting of of the double tower gas fractionator that is mainly formed by depropanizing tower and propylene distillation tower, referring to Fig. 1 as can be known, the charging of depropanizing tower 1 is extracted liquid hydrocarbon by liquid hydrocarbon pump 2 in liquid hydrocarbon tank 3, top of tower is provided with the first condenser 4, the first return tank 5 and the first reflux pump 6, make the gas at its top after 4 condensations of the first condenser, be back to the first return tank 5, by the first reflux pump 6 the condensation liquid phase part is sent into depropanizing tower 1 cat head afterwards, part is squeezed into propylene rectification tower 7 opening for feeds;
The bottom of depropanizing tower 1 is provided with reflux pump 9 at the bottom of the first reboiler 8 and the first tower, so that the liquid phase of the bottom of depropanizing tower 1 is back in the depropanizing tower 1 after reflux pump 9 parts are delivered to the first reboiler 8 at the bottom of the first tower, another part is as the mixed c 4 take-off equipment;
The top of described propylene rectification tower 7 is provided with the second condenser 10, the second return tank 11 and the second reflux pump 12, make the gas phase at its top after the second condenser 10 is condensed into liquid phase, be back to the second return tank 11, by the second reflux pump 12 a liquid phase part is back in the propylene rectification tower 7 afterwards; Another part is as output of products;
The bottom of propylene rectification tower 7 is provided with reflux pump 14 at the bottom of the second reboiler 13 and the second tower, so that the liquid phase of the bottom of propylene rectification tower 7 is back in the propylene rectification tower 7 after delivering to the second reboiler 13 through reflux pump 14 parts at the bottom of the second tower, another part is as output of products;
When in step 1) in measure the C that comprises in the liquid hydrocarbon
2In interior light constituent and propylene molar content than whether less than 0.003 or 0.0024 o'clock, lower for the requirement meeting of energy consumption, more be conducive to directly in liquid hydrocarbon, isolate propylene and propane by above-mentioned double tower gas fractionator.
In the sepn process, by regulating C in the discharging of reflux ratio restriction depropanizing tower cat head
4Content is to guarantee the rectifying tower quality product, quantity of reflux restriction depropanizing tower tower reactor C at the bottom of the control tower
3Content is to guarantee the propylene tower product yield;
When liquid hydrocarbon does not satisfy the new technological process requirement, also can directly incorporate deethanizing column into device, be about to depropanizing cat head material and introduce the deethanizing column opening for feed, liquid phase at the bottom of the deethanizing column is introduced the conversion that the propylene rectification tower opening for feed can be realized old flow process.
Now above technical scheme is carried out Simulation and analysis:
1, material balance-C
2 -The preliminary of content determined
The design of any flow process all will in the gas separation unit, make propylene product purity 〉=99.6% from material balance, comprise C
2Be C at interior impurity
2 -Content is no more than 0.4% (χ), i.e. C
2 -/ C
3 =＜0.004.Propylene content is 25%～40% (χ) in the general liquid hydrocarbon, and propene yield calculates by 100%, for there not being the deethanizing column double-column process, in the charging with C
2Meter light constituent content should be lower than 0.1%～0.16% (χ), requires C in the gas separation unit charging
2 -Content is low guarantee quality product enough.
2, new technological process simulation
According to above-mentioned analysis, take industrial actual production data as reference, the liquid hydrocarbon of selecting to satisfy double-column process enforcement basis carries out the double-column process simulation, and table 7 is depicted as 5 kinds of different liquid hydrocarbons that form.
2.1 process stipulation
Depropanizing tower (T1):
Tower reactor C
3≤ 1% (χ), cat head C
4≤ 0.5% (χ);
Propylene tower is propylene rectification tower (T3):
Cat head propylene product purity 〉=99.6% (χ), tower reactor propane product purity 〉=97.0% (χ).
2.2 operational condition
Simulation process adopts the SRK equation, and initial operational parameters is take table 2 as reference.
Table 7 gas separation unit liquid hydrocarbon forms % (χ)
| Form | |
|
|
Liquid hydrocarbon 8 | Liquid hydrocarbon 9 |
| C 2 - | 0.03 | 0.076 | 0.100 | 0.12 | 0.14 |
| C 3 ＝ | 41.91 | 39.55 | 34.70 | 33.73 | 35.89 |
| C 3 0 | 8.80 | 5.14 | 9.30 | 13.66 | 8.93 |
| i-C 4 0 | 12.68 | 12.01 | 21.70 | 23.65 | 23.92 |
| n-C 4 0 | 4.39 | 3.89 | 4.20 | 6.59 | 7.22 |
| C 4 ＝-1 | - | 8.43 | 4.20 | 6.01 | 4.22 |
| i-C 4 ＝ | 18.48 | 12.14 | 11.50 | 7.00 | 13.55 |
| t-C 4 ＝-2 | 5.50 | 7.76 | 7.10 | 3.76 | 5.99 |
| c-C 4 ＝-2 | 8.17 | 9.95 | 7.10 | 5.47 | 0.00 |
| C 5 + | 0.04 | 1.06 | 0.10 | 0.01 | 0.12 |
| C 2 -/C 3 ＝(χ) | 0.0007 | 0.0019 | 0.0029 | 0.0036 | 0.0039 |
2.3 flowsheeting explanation and interpretation of result
For guaranteeing propylene tower tower reactor propane quality, need depropanizing cat head flow C
4Content limits, take liquid hydrocarbon 1 as example, and depropanizing cat head C
4Content should be less than 0.4% (χ), guarantee propane product purity.By optimizing double-column process two tower reflux ratios, feed entrance point, all can obtain qualified propylene, propane product, and yield is respectively 99%, (see Table 8) more than 96%.
Analog result sees Table 8, and on the basis of same operation pressure, separation progression, separation accuracy, the size of reflux ratio has reflected the complexity of product separation, and Fig. 2 is different C
2 -/ C
3 =Liquid hydrocarbon reflux ratio, reboiler changing conditions are along with C
2 -/ C
3 =Increase, two tower reflux ratios, energy consumption all increase to some extent, and wherein the variation of propylene cat head accounts for leading; In the liquid hydrocarbon 8,9, because C
2Following light constituent relative content is higher, and propylene product limited purity system needs as far as possible the restructuring such as top pronane to be divided condensation, are separated to tower reactor for this reason, causes propylene tower reflux ratio, reboiler to increase substantially, and loses more than gain.
3, liquid hydrocarbon forms the impact analysis to two tower operational conditions, phase load
Fig. 3, Fig. 4 are different C
2 -/ C
3 =, C
3 =/ C
3 0The relation of liquid hydrocarbon and propylene tower reflux ratio, propylene product yield is by liquid towards hydrocarbon C
2 -/ C
3 =, C
3 =/ C
3 0Variation is learnt the impact analysis of two tower operational conditions, C
2 -/ C
3 =On the impact of propylene tower operational condition significantly, C
3 =/ C
3 0A little less than the impact of propylene tower operational condition.Among Fig. 3, work as C
2 -/ C
3 ==0.003 is knee point, C in liquid hydrocarbon
2 -/ C
3 =Greater than 0.003 o'clock, propylene tower reflux ratio, yield sharply rose, and double-column process is difficult for realizing stable, economic operation.
Fig. 5, Fig. 6 are different C
2 -/ C
3 =C is worked as in propylene tower vapour phase load, condenser and reboiler contrast in lower three-column process flow, the double-column process
2 -/ C
3 =Be lower than at 0.0024 o'clock, vapour phase load, condenser and reboiler change all in design capacity in the tower.Be that double-column process can be transformed based on former three-column process flow, propylene tower still can keep good vapour-liquid mass, satisfies the specification of quality that separates.
4, application
According to above-mentioned analysis, C in liquid hydrocarbon
2 -/ C
3 =Be lower than at 0.0024 o'clock, do not change tower, interchanger, deethanizing column is cut out gas separation unit (three-column process flow), the depropanizing tower overhead stream directly advances propylene rectification tower to be separated and can realize double-column process technique.When in recent years, domestic catalytic cracking unit is by Optimizing operation, C in the liquid hydrocarbon
2 -Concentration continues to reduce (seeing Table 9), for double tower gas division technique provides qualified liquid hydrocarbon.
In above simulation process, regulation propylene, propane quality product (χ) are respectively 99.6%, 97.0%, and as optimization aim, process stipulation is very strict to improve product yield (being respectively 99%, 96%).In the actual production process, large multiple enterprises gas separation unit only requires propylene quality and yield, to the sometimes no requirement (NR) of propane quality, but with thick propane and mixed c 4 in the lump as the civil liquefied gas commodity.So, double-column process is transformed the requirement that the liquid towards hydrocarbon forms, heat-exchange equipment is loaded and can be decreased, and its suitability is more wide in range.
The industrial gas separation unit liquid hydrocarbon of table 9 forms example % (χ)
| Component | Breathe out petrochemical industry | Front Guo Shihua | The Fushun petrochemical industry | Only petrochemical industry | The pagoda petrochemical industry |
| C 2 - | 0.02 | 0.03 | 0.04 | 0.05 | 0.076 |
| C 3 ＝ | 33.5 | 26.91 | 29.36 | 37.87 | 39.547 |
| C 3 0 | 11.0 | 8.04 | 8.42 | 12.38 | 5.14 |
| i-C 4 0 | 21.8 | 24.77 | 21.45 | 18.51 | 12.014 |
| n-C 4 0 | 5.6 | 8.16 | 5.57 | 5.76 | 3.887 |
| C 4 ＝-1 | 6.8 | 7.10 | - | 14.17 | 8.434 |
| i-C 4 ＝ | 10.3 | 9.37 | 16.86 | 4.54 | 12.138 |
| t-C 4 ＝-2 | 4.3 | 6.30 | 6.50 | 6.72 | 7.757 |
| c-C 4 ＝-2 | 6.5 | 9.08 | 9.20 | - | 9.946 |
| C 5 + | 8.16 | 0.24 | 2.60 | - | 1.062 |
| C 2 -/C 3 ＝(χ) | 0.0006 | 0.0011 | 0.0014 | 0.0013 | 0.0019 |
Claims (4)
1. the method for separation of propylene and propane in a liquid hydrocarbon is characterized in that the method may further comprise the steps:
1) measures the C that comprises in the liquid hydrocarbon
2Be C at interior light constituent
2 -Whether content compares less than 0.004 with the propylene molar content, if so, carry out step 2);
2) double tower gas fractionator by mainly being comprised of depropanizing tower and propylene rectification tower is isolated high-purity propylene and qualified propane in above-mentioned liquid hydrocarbon; The formation of described double tower gas fractionator is that the opening for feed of depropanizing tower extracts liquid hydrocarbon by liquid hydrocarbon pump from the liquid hydrocarbon tank, its top is provided with the first condenser, the first return tank and the first reflux pump, make the gas phase at its top after the first condenser condenses, be back to the first return tank, by the first reflux pump a condensation liquid phase part is sent into again rectifying of depropanizing tower afterwards, another part is squeezed into the propylene rectification tower opening for feed;
Depropanizing tower bottom is provided with reflux pump at the bottom of reboiler and the first tower, be back in the depropanizing tower after the first reboiler is heated to certain temperature so that depropanizing tower tower reactor liquid phase is delivered to through a reflux pump part at the bottom of the first tower, another part is as mixed c 4 output of products device; It is for rectifying tower provides thermal source that reboiler one is set at the bottom of the tower, the 2nd, and C at the bottom of the control tower
3Balanced contents is avoided carrying excessive C at the bottom of the tower
3Affect propylene, propane product yield as the output of the mixed c 4 of cheapness;
Described propylene rectification tower structure is similar with depropanizing tower, its top is provided with the second condenser, the second return tank and the second reflux pump, top gaseous phase is back to the second return tank through the second condenser condenses, be back in the propylene rectification tower by the second reflux pump afterwards, another part is exported as propylene product;
The bottom of propylene rectification tower is provided with reflux pump at the bottom of the second reboiler and the second tower, so that propylene rectification tower tower reactor part liquid phase is back in the propylene rectification tower after reflux pump is partly delivered to the second reboiler at the bottom of the second tower, another part is as output of products.
As claimed in claim 1 in liquid hydrocarbon the method for separation of propylene and propane, it is characterized in that: in step 1) in measure in the liquid hydrocarbon and comprise C
2Whether compare less than 0.003 in interior light constituent and propylene molar content.
As claimed in claim 1 or 2 in liquid hydrocarbon the method for separation of propylene and propane, it is characterized in that: in step 1) in measure in the liquid hydrocarbon and comprise C
2Whether compare less than 0.0024 in interior light constituent and propylene molar content.
As claimed in claim 3 in liquid hydrocarbon the method for separation of propylene and propane, it is characterized in that: in the sepn process, by regulating C in the discharging of reflux ratio restriction depropanizing tower cat head
4Content is to guarantee the rectifying tower quality product, quantity of reflux restriction depropanizing tower tower reactor C at the bottom of the control tower
3Content is to guarantee the propylene rectification tower product yield.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104193575A (en) * | 2014-09-11 | 2014-12-10 | 中建安装工程有限公司 | Device and method for extracting, distilling and separating propane and propylene |
| CN107011110A (en) * | 2017-05-19 | 2017-08-04 | 张家港市华昌新材料科技有限公司 | The method for separating propylene propane |
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| CN107011110A (en) * | 2017-05-19 | 2017-08-04 | 张家港市华昌新材料科技有限公司 | The method for separating propylene propane |
| CN107011110B (en) * | 2017-05-19 | 2023-11-03 | 张家港市华昌新材料科技有限公司 | Method for separating propylene propane |
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