CN203079876U - Olefin separation system - Google Patents
Olefin separation system Download PDFInfo
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- CN203079876U CN203079876U CN201320045987XU CN201320045987U CN203079876U CN 203079876 U CN203079876 U CN 203079876U CN 201320045987X U CN201320045987X U CN 201320045987XU CN 201320045987 U CN201320045987 U CN 201320045987U CN 203079876 U CN203079876 U CN 203079876U
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Abstract
The utility model provides an olefin separation system. The olefin separation system comprises a demethanization unit, wherein the demethanization unit comprises a primary demethanization tower, a membrane separation assembly and a secondary demethanization tower; a first gas phase material flow pipeline is arranged between a tower top outlet of the primary demethanization tower and an inlet of the membrane separation assembly; and a hydrocarbon-rich gas flow pipeline is arranged between a hydrocarbon-rich gas flow outlet of the membrane separation assembly and an inlet of the secondary demethanization tower. The olefin separation system has the beneficial effects that the first gas phase material flow is obtained by carrying out non-clear or clear cutting on the gas to be separated by the primary demethanization tower and is further separated into hydrocarbon-rich gas flow and hydrogen-rich gas flow by the membrane separation assembly, thus increasing the ratio of molecules CH4/H2 in the hydrocarbon-rich gas flow entering the secondary demethanization tower, further increasing the partial pressure of CH4 on the top of the secondary demethanization tower and reducing the energy consumption needed for reducing the temperature and the investment and operating costs of olefin separation.
Description
Technical field
The utility model relates to the gas delivery field, in particular to a kind of olefin separation system.
Background technology
In oil gas, oil refinery dry gas and the methanol-to-olefins product gas except that containing ethene, propylene, also contain a large amount of other compositions, as hydrogen, methane, acetylene, propane and nitrogen etc., because ethene, propylene are important chemical material, therefore can adopt above oil gas, oil refinery dry gas and methanol-to-olefins product gas is that raw material separates ethene and propylene wherein, at present, deep cooling separating method is the most ripe, adopts at most.
There are many shortcomings in typical conventional deep cooling separating method, such as requiring usually unstripped gas is carried out 4 to 5 grades of compressions, need a large amount of low-temperature cooling medias, separating the refrigeration system that needs below-100 ℃ as methane-hydrogen cools off, therefore, the energy consumption of conventional deep cooling separating method is higher, and is also high to the requirement of equipment, and the separating effect that wants to realize ideal has to strengthen investment.In the low temperature separation process process, hydrogen and methane separation are maximum one of energy consumption and cost consumption in the entire separation system, and complex process.Because, CH in the unstripped gas
4/ H
2Molecule ratio is very big to ethylene loss influence in the tail gas, and this is because H because of the demethanizing tower item
2Reduced CH with the existence of other rare gas element
4Dividing potential drop has only pressurize or reduction temperature just to satisfy the requirement of cat head to dew point, and pressurize and reduction temperature are being isolated CH
4The time, part ethene also can with CH
4Together be separated, cause the loss of ethene, above-mentioned influence is by the decision that balances each other, and stage number and reflux ratio what do not depend on, therefore at temperature and pressure condition one timing, CH in the unstripped gas
4/ H
2Molecule ratio is littler, and ethylene loss is just bigger in the tail gas, otherwise then little, energy consumption is also low more.Therefore, how from splitting gas or olefine mixing gas, separate hydrogen is as much as possible, cause people's extensive concern with the energy consumption that reduces the hydrogen methane separation.
Existing Lu Musi technology is one of technology more advanced in the separation of deep cooling alkene, the structural representation of Lu Musi alkene low temperature separation process system as shown in Figure 1: enter depropanizing tower 51 ' after the unstripped gas drying device 52 ' drying, the cat head gas phase of depropanizing tower 51 ' is separated through the laggard promoting the circulation of qi liquid of the unitary overhead condenser 54 ' partial condensation of depropanizing, the liquid that condensation is got off is as the backflow of depropanization system, all the other gas phases that contain carbon three hydro carbons and carbon three following hydrocarbon components enter compressor 53 ' boost after, successively through second reboiler 192 ', enter demethanizing tower 11 ' after the first cryogen chiller 161 ' and the second cryogen chiller, 162 ' a series of heat exchange process of cooling; Depropanizing tower 51 ' bottom product is that carbon four and carbon four above components are sent to debutanizing tower 61 '.The unitary overhead condenser of demethanizing utilizes propylene (or ethene) to make cryogen, the overhead stream of partial condensation enters (unitary overhead condenser of not shown demethanizing and return tank among Fig. 1) behind the return tank, the liquid phase that return tank is separated is as the backflow of demethanizing tower 11 ', gas phase is (based on hydrogen and methane, be called the hydrogen methane gas stream) through after the ice chest 142 ' heat exchange, deliver to the outer gas ductwork of device.The logistics that contains C2 hydrocarbon class and carbon three hydrocarbon compositions at the bottom of the demethanizing tower 11 ' tower enters deethanizing column 31 ', the overhead stream of deethanizing column 31 ' passes through at first that hydrogenation acetylene removal reactor 21 ' changes into ethene with the alkynes class in the logistics (mainly being acetylene) and ethane enters ethylene rectification tower 22 ' then, the cat head gas phase of ethylene rectification tower 22 ' is as ethylene product feeder tank field, and ethane is sent into fuel gas system and acted as a fuel and use or recycle and handle at the bottom of the tower of ethylene rectification tower 22 ' after interchanger heating vaporization.The tower base stream of deethanizing column 31 ' enters the propylene rectification cell; the cat head propylene product of propylene rectification tower 41 ' refluxes the Partial Liquid Phase material through return tank of top of the tower 42 ' through overhead water cooler 43 ' condensation rear section; remove behind methyl alcohol, oxide compound and other impurity as propylene product feeder propylene tank field, partial reflux propylene rectification tower 41 ' through product protection bed (not shown in figure 1) again.Propane logistics at the bottom of the propylene rectification tower 41 ' tower is through ice chest 142 ' and hydrogen methane gas stream heat exchange cooling, the methane that the cat head of introducing demethanizing tower 11 ' is located with absorption demethanizing tower 11 ' after the 3rd cryogen chiller 163 ' is by the cryogen Quench, the ethene in the hydrogen gas stream; Entering gas ductwork after another stock-traders' know-how ice chest 142 ' heat exchange uses as combustion gas.The material of isolated carbon containing four of propylene rectification cell and above component enters debutanizing tower 61 ' and separates carbon four hydro carbons and carbon four above hydrocarbon productss.
Above-mentioned conventional cryogenics and Lu Musi technology are owing to all be to adopt a demethanizing to handle the molecule ratio that is difficult to obtain ideal methane and hydrogen, therefore cause tail gas in the process of separating ethene the energy consumption height, the ethylene loss amount is big and invest high shortcoming, the utility model mainly is the improvement of in order to realize cutting down the consumption of energy, reduce ethylene loss the Lu Musi technology being made on the basis of Lu Musi technology.
The utility model content
The utility model aims to provide a kind of olefin separation system, has reduced the energy consumption in the olefin separation process.
To achieve these goals, according to an aspect of the present utility model, a kind of olefin separation system is provided, this olefin separation system comprises the demethanizing unit, the demethanizing unit comprises just demethanizing tower, membrane separation assemblies and inferior demethanizing tower, is provided with the first gaseous stream pipeline between the tower top outlet of first demethanizing tower and the import of membrane separation assemblies; Be provided with rich hydrocarbon stream pipeline between the rich hydrocarbon stream outlet of membrane separation assemblies and the import of time demethanizing tower.
Further, above-mentioned demethanizing unit also comprises first compressor, first ice chest, first interchanger, second interchanger, first cryogen chiller and the decompressor, has the second gaseous stream pipeline between the tower top outlet of inferior demethanizing tower and the import of decompressor; First compressor is arranged on the rich hydrocarbon stream pipeline; First ice chest has: stream in first gaseous stream, first ice chest is serially connected in the first gaseous stream pipeline; Stream in rich hydrocarbon stream first ice chest is serially connected in the rich hydrocarbon stream pipeline between the import of first compressor and inferior demethanizing tower; First interchanger has: stream in rich hydrocarbon stream first interchanger is serially connected in the rich hydrocarbon stream pipeline between the import of stream and inferior demethanizing tower in rich hydrocarbon stream first ice chest; Stream in second liquid phase stream, first interchanger is connected with the tower bottom outlet of inferior demethanizing tower, and the rich hydrocarbon stream and second liquid phase stream carry out heat exchange in first interchanger; Second interchanger has: stream in rich hydrocarbon stream second interchanger is serially connected in the rich hydrocarbon stream pipeline between the import of stream and inferior demethanizing tower in rich hydrocarbon stream first interchanger; Stream in second gaseous stream, second interchanger is connected with the outlet of decompressor, and the rich hydrocarbon stream and second gaseous stream carry out heat exchange in second interchanger; The first cryogen chiller is arranged between the import of interior stream of rich hydrocarbon stream second interchanger and time demethanizing tower.
Further, above-mentioned demethanizing unit also comprises: first reboiler, and being connected with the first tower bottom outlet of first demethanizing tower and linking to each other with the tower still of first demethanizing tower forms first circulation line; Second reboiler, being connected with the second tower bottom outlet of first demethanizing tower and linking to each other with the tower still of first demethanizing tower forms second circulation line.
Further, above-mentioned olefin separation system also comprises the ethylene distillation unit, and the ethylene distillation unit comprises: hydrogenation acetylene removal reactor has: the hydrogen gas stream import, and have the hydrogen rich stream pipeline between the outlet of the hydrogen rich stream of membrane separation assemblies; The hydrocarbon material import, and have the second liquid phase stream pipeline between the tower bottom outlet of inferior demethanizing tower; The ethylene product outlet; Ethylene rectification tower is connected with the ethylene product outlet.
Further, above-mentioned olefin separation system also comprises deethanizing unit and propylene rectification cell, the deethanizing unit comprises deethanizing column, and deethanizing column has: the first liquid phase stream import, and have the first liquid phase stream pipeline between the 3rd tower bottom outlet of first demethanizing tower; The deethanizer overhead stream outlet, and have hydro carbons acetylene removal mass transport pipeline between the hydrocarbon material import of hydrogenation acetylene removal reactor; The propylene rectification cell comprises: propylene rectification tower has: the 3rd liquid phase stream import, and have the 3rd liquid phase stream pipeline between the tower bottom outlet of deethanizing column; The outlet of cat head propylene; Return tank of top of the tower is connected with the outlet of the cat head propylene of propylene rectification tower and constitutes the 3rd circulation line with propylene rectification tower, and first reboiler or second reboiler have propylene import and the propylene outlet that is connected with the 3rd circulation line.
Further, also be provided with control valve on the 3rd circulation line between aforesaid propylene rectifying tower and the return tank of top of the tower, the control valve and first reboiler or second reboiler are arranged in parallel.
Further, above-mentioned olefin separation system also comprises second ice chest, and second ice chest has the second gas phase liquid and flows stream in second ice chest, and the second gas phase liquid flows the interior stream of second ice chest and is connected with the interior stream of second gaseous stream, second interchanger of second interchanger; Have two article of the 4th liquid phase stream pipeline between the propylene rectification tower and second ice chest, be connected with gas ductwork after one article of the 4th liquid phase stream pipeline wherein passes second ice chest; Another article the 4th liquid phase stream pipeline passes to extend to behind second ice chest with first demethanizing tower and is connected, olefin separation system also comprises the second cryogen chiller, and the second cryogen chiller is arranged on second ice chest and just on the 4th liquid phase stream pipeline between the demethanizing tower.
Further, above-mentioned olefin separation system also comprises: the depropanizing unit comprises: depropanizing tower, the tower top outlet of depropanizing tower with just be provided with the logistics pipeline mutually of the degassing just between the demethanizing tower; Moisture eliminator is connected with the import of depropanizing tower and carries unstripped gas to be separated to depropanizing tower; Second compressor is arranged on depropanizing tower and the first degassing between the demethanizing tower just mutually on the logistics pipeline; The 3rd cryogen chiller, be arranged on second compressor and the first degassing between the demethanizing tower just mutually on the logistics pipeline, first ice chest have with second compressor and the 3rd cryogen chiller between the first degassing mutually the first degassing phase logistics import and the degassing phase logistics just that are connected of logistics pipeline export; The debutylize unit comprises: debutanizing tower, and be provided with the first liquid phase stream pipeline that takes off between the depropanizing tower; Overhead condenser has the import and the cooling that are connected with the tower top outlet of debutanizing tower and coagulates the effusive outlet of after product.
Use the technical solution of the utility model, first demethanizing tower, membrane separation assemblies and time demethanizing tower coordinating operation, through after the sub-zero treatment of first demethanizing tower, just the cat head working temperature of demethanizing tower and pressure are treated gas separated and are carried out non-clear cutting or clear cutting by the control rationally of temperature control component and pressure control valve, not carbon containing three that obtains after gas to be separated is handled through first demethanizing tower and first gaseous stream of carbon three above hydro carbons further are divided into rich hydrocarbon stream and hydrogen rich stream with first gaseous stream effectively through after the separation of membrane separation assemblies, have increased the CH in the rich hydrocarbon stream that enters time demethanizing tower
4/ H
2Molecule ratio, and then increased the inferior demethanizer column overhead CH of place
4Dividing potential drop, therefore only the temperature of inferior demethanizing tower need be reduced to higher dew point and can isolate CH
4And H
2, the required energy consumption of cooling has reduced in sepn process so; And, because increasing of dew point makes to have only seldom or even do not have ethene in time isolating second gaseous stream of demethanizer column overhead, therefore reduced the loss of ethene; Simultaneously, the realization of above-mentioned technique effect can significantly reduce isolating investment of alkene and running cost.
Description of drawings
The Figure of description that constitutes the application's a part is used to provide further understanding of the present utility model, and illustrative examples of the present utility model and explanation thereof are used to explain the utility model, do not constitute improper qualification of the present utility model.In the accompanying drawings:
Fig. 1 shows the structural representation according to the Lu Musi alkene low temperature separation process system of prior art; And
Fig. 2 shows the structural representation according to the olefin separation system in a kind of preferred embodiment of the present utility model.
Embodiment
Need to prove that under the situation of not conflicting, embodiment and the feature among the embodiment among the application can make up mutually.Describe the utility model below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
As shown in Figure 2, in a kind of typical embodiment of the utility model, a kind of olefin separation system is provided, this olefin separation system comprises the demethanizing unit, the demethanizing unit comprises just demethanizing tower 11, membrane separation assemblies 12 and inferior demethanizing tower 17, is provided with the first gaseous stream pipeline between the tower top outlet of the first demethanizing tower 11 of membrane separation assemblies and the import of membrane separation assemblies 12; Be provided with rich hydrocarbon stream pipeline between the import of the tower top outlet of membrane separation assemblies 12 and time demethanizing tower 17.
Olefin separation system with said structure, adopt demethanizing tower 11 just, membrane separation assemblies 12 and time demethanizing tower 17 are used, through after the sub-zero treatment of first demethanizing tower 11, the cat head working temperature of the first demethanizing tower 11 of reasonable control and pressure are treated gas separated and are carried out non-clear cutting or clear cutting, obtain after gas to be separated is handled through first demethanizing tower 11 not that first gaseous stream of carbon containing three and carbon three above hydro carbons further is divided into rich hydrocarbon stream and hydrogen rich stream with first gaseous stream effectively through after the separation of membrane separation assemblies 12, increased the CH in the rich hydrocarbon stream that enters time demethanizing tower 17
4/ H
2Molecule ratio, and then increased inferior demethanizing tower 17 CH of cat head place
4Dividing potential drop, therefore only the temperature of inferior demethanizing tower 17 need be reduced to higher dew point and can isolate CH
4And H
2, the required energy consumption of cooling has reduced in sepn process so; And, owing to increasing of dew point makes that only needing lower cold just can make has only seldom or even do not have ethene in time isolating second gaseous stream of demethanizing tower 17 cats head, has therefore reduced the loss of ethene; Simultaneously, the realization of above-mentioned technique effect can significantly reduce the isolating investment of alkene.
As shown in Figure 2, in a kind of preferred embodiment of the utility model, above-mentioned demethanizing unit also comprises first compressor 131, first ice chest 141, first interchanger 151, second interchanger 152, the first cryogen chiller 161 and decompressor 18, has the second gaseous stream pipeline between the import of the tower top outlet of inferior demethanizing tower 17 and decompressor 18; First compressor 131 is arranged on the rich hydrocarbon stream pipeline; First ice chest 141 has stream and the interior stream of rich hydrocarbon stream first ice chest in first gaseous stream, first ice chest, and stream is serially connected in the first gaseous stream pipeline in first gaseous stream, first ice chest; Stream is serially connected in the rich hydrocarbon stream pipeline between the import of first compressor 131 and inferior demethanizing tower 17 in rich hydrocarbon stream first ice chest; First interchanger 151 has in rich hydrocarbon stream first interchanger stream in the stream and second liquid phase stream, first interchanger, and stream is serially connected in the rich hydrocarbon stream pipeline between the import of stream and inferior demethanizing tower 17 in rich hydrocarbon stream first ice chest in rich hydrocarbon stream first interchanger; Stream is connected with the tower bottom outlet of time demethanizing tower 17 in second liquid phase stream, first interchanger, and the rich hydrocarbon stream and second liquid phase stream carry out heat exchange in first interchanger 151; Second interchanger 152 has in rich hydrocarbon stream second interchanger stream in the stream and second gaseous stream, second interchanger, and stream is serially connected in the rich hydrocarbon stream pipeline between the import of stream and inferior demethanizing tower 17 in rich hydrocarbon stream first interchanger in rich hydrocarbon stream second interchanger; Stream is connected with the outlet of decompressor 18 in second gaseous stream, second interchanger, and the rich hydrocarbon stream and second gaseous stream carry out heat exchange in second interchanger 152; The first cryogen chiller 161 is arranged between the import of interior stream of rich hydrocarbon stream second interchanger and time demethanizing tower 17.
In above-mentioned olefin separation system, reduce from the rich hydrocarbon stream of membrane separation assemblies 12 temperature after in first ice chest 141, carrying out heat exchange with first gaseous stream after the 131 compression superchargings of first compressor, enter first interchanger 151 and heat-eliminating medium then and carry out continuing after the heat exchange once more entering temperature reduction after the second gaseous stream heat exchange that second interchanger 152 and the back temperature that expands through decompressor 18 sharply descend from first demethanizing tower 11; Rich subsequently hydrocarbon stream continue to enter the first cryogen chiller 161 and cryogen carry out heat exchange further cooling enter time demethanizing tower 17 with lower temperature and carry out low temperature separation process once more, a series of heat exchange that rich hydrocarbon stream is carried out are reduced temperature significantly, have further reduced the energy consumption of low temperature separation process in the inferior demethanizing tower 17.
As shown in Figure 2, the demethanizing unit comprises also that first reboiler 191 and second reboiler, 192, the first reboilers 191 are connected with the first tower bottom outlet of first demethanizing tower 11 and links to each other with the tower still of first demethanizing tower 11 and forms first circulation line; Second reboiler 192 is connected with the second tower bottom outlet of first demethanizing tower 11 and links to each other with the tower still of first demethanizing tower 11 and forms second circulation line.
Part becomes gas phase by the first tower bottom outlet of first demethanizing tower 11 and effusive first liquid phase stream of the second tower bottom outlet and returns in the tower still of first demethanizing tower 11 after first reboiler 191 or 192 heating of second reboiler, and with the reverse contact mass transfer of the liquid phase stream that stays by cat head, reach the purpose of cryogenic rectification.
As shown in Figure 2, olefin separation system also comprises the ethylene distillation unit, the ethylene distillation unit comprises hydrogenation acetylene removal reactor 21 and ethylene rectification tower 22, hydrogenation acetylene removal reactor 21 has hydrogen gas stream import, hydrocarbon material import and ethylene product outlet, has the hydrogen rich stream pipeline between the hydrogen rich stream outlet of hydrogen gas stream import and membrane separation assemblies 12; Has the second liquid phase stream pipeline between the tower bottom outlet of hydrocarbon material import and time demethanizing tower 17; Ethylene rectification tower 22 is connected with the ethylene product outlet.
Carrying out after the heat exchange temperature by isolated second liquid phase stream based on the C2 hydrocarbon class of inferior demethanizing tower 17 as the heat-eliminating medium of first interchanger 151 and first gaseous stream raises and then enters hydrogenation acetylene removal reactor 21 and carry out hydrogenation reaction, hydrogen derives from membrane separation assemblies 12 isolated hydrogen rich streams and/or external hydrogen in hydrogenation acetylene removal reactor 21, and the material that obtains after hydrogenation is finished forms ethylene product after ethylene rectification tower 22 rectifying.Separated hydrogen is rationally utilized, reduced the external hydrogen gas consumption of acetylene hydrogenation, saved the acetylene hydrogenation cost.
As shown in Figure 2, olefin separation system also comprises deethanizing unit and propylene rectification cell, the deethanizing unit comprises deethanizing column 31, deethanizing column 31 has the first liquid phase stream import and deethanizer overhead stream outlet, has the first liquid phase stream pipeline between the 3rd tower bottom outlet of the first liquid phase stream import and first demethanizing tower 11; Has hydro carbons acetylene removal mass transport pipeline between the hydrocarbon material import of deethanizer overhead stream outlet and hydrogenation acetylene removal reactor 21; The propylene rectification cell comprises propylene rectification tower 41 and return tank of top of the tower 42, and propylene rectification tower 41 has the 3rd liquid phase stream import and the outlet of cat head propylene, has the 3rd liquid phase stream pipeline between the tower bottom outlet of the 3rd liquid phase stream import and deethanizing column 31; Return tank of top of the tower 42 is connected with the outlet of the cat head propylene of propylene rectification tower 41 and constitutes the 3rd circulation line with propylene rectification tower 41, and first reboiler 191 or second reboiler 192 have propylene import and the propylene outlet that is connected with the 3rd circulation line.
In above-mentioned olefin separation system, what just demethanizing tower 11 isolated first liquid phase streams were handled back formation through deethanizing column 31 is the charging that the ethene gas mixture of main component can be used as hydrogenation acetylene removal reactor 21 with ethene, to remove a small amount of alkynes type organic wherein; Simultaneously because time demethanizing tower 17 isolated second liquid phase streams nearly all are C-2-fraction, so this burst logistics need not to enter deethanizing column 31, having only first liquid phase stream that first demethanizing tower 11 contains carbon two and carbon three components to enter deethanizing column 31 separates, thereby alleviated the load of deethanizing column 31 greatly, helped reducing the energy consumption and the investment cost of deethanizing column 31; Deethanizing column 31 isolated the 3rd liquid phase streams based on propylene enter cat head propylene product that propylene rectification tower 41 carries out obtaining after the rectifying and enter unitary first reboiler 191 of demethanizing or second reboiler 192 and first liquid phase stream and carry out lowering the temperature after the heat exchange, the heat of while cat head propylene product is become gas phase by first liquid phase stream absorption back, first liquid phase stream and returns in the tower still of first demethanizing tower 11, and with the reverse contact mass transfer of the liquid phase stream that stays by cat head, the purpose that reaches cryogenic rectification utilizes the alternative hot steam of cat head propylene product and first liquid phase stream to carry out heat exchange like this in first reboiler 191 or second reboiler 192, remaining heat and cold in the system have been made full use of, reduced the consumption of hot steam and water, save energy consumption and water resources, saved the use of water coolant and the facility investment of overhead water cooler.Cooled cat head propylene product obtains qualified propylene product after removing wherein a spot of methyl alcohol, oxide compound and other impurity through devices such as product protection beds.
For heat exchange and adjusting demethanizing tower 11 operations (as service temperature) just of controlling the cat head propylene product effectively, as shown in Figure 2, also be provided with control valve 43 on the 3rd circulation line between propylene rectification tower 41 and the return tank of top of the tower 42, the control valve 43 and first reboiler 191 or second reboiler 192 are arranged in parallel, in order to the flow through amount of propylene product of first reboiler 191 or second reboiler 192 of adjusting.
As shown in Figure 2, olefin separation system also comprises second ice chest 142, second ice chest 142 has the second gas phase liquid and flows stream in second ice chest, and the second gas phase liquid flows the interior stream of second ice chest and is connected with the interior stream of second gaseous stream, second interchanger of second interchanger 152; Have two article of the 4th liquid phase stream pipeline between the propylene rectification tower 41 and second ice chest 142, one article of the 4th liquid phase stream pipeline wherein passes second ice chest, 142 backs and is connected with gas ductwork; Another article the 4th liquid phase stream pipeline passes to extend to behind second ice chest 142 with first demethanizing tower 11 and is connected, olefin separation system comprises also that the second cryogen chiller, 162, the second cryogen chillers 162 are arranged on second ice chest 142 and just on the 4th liquid phase stream pipeline between the demethanizing tower 11.
In above-mentioned olefin separation system, cool off through decompressor 18 expansions by second gaseous stream from inferior demethanizing tower 17, in second ice chest 142, cool off the 4th liquid phase stream after the cooling of the rich hydrocarbon stream that passes through in second interchanger 152 as heat-eliminating medium, on the one hand second gaseous stream temperature after heat exchange rises to some extent and transfers out the olefin separation system use that acts as a fuel, cooled on the other hand part the 4th liquid phase stream enters first demethanizing tower 11 again after the second cryogen chiller, 162 further Quench cat head partly is used for absorbing the ethene of cat head place first gaseous stream of demethanizing tower 11 just, and another part the 4th liquid phase stream can be sent into gas ductwork and use as combustion gas.
As shown in Figure 2, olefin separation system also comprises depropanizing unit and debutylize unit, the depropanizing unit comprises depropanizing tower 51, moisture eliminator 52, second compressor 132 and the 3rd cryogen chiller 163, the tower top outlet of depropanizing tower 51 with just be provided with the logistics pipeline mutually of the degassing just between the demethanizing tower 11; Moisture eliminator 52 is connected with the import of depropanizing tower 51 and carries unstripped gas to be separated to depropanizing tower 51; Second compressor 132 is arranged on depropanizing tower 51 and the first degassing between the demethanizing tower 11 just mutually on the logistics pipeline; The 3rd cryogen chiller 163 is arranged on second compressor 132 and the first degassing between the demethanizing tower 11 just mutually on the logistics pipeline, first ice chest 141 have with second compressor 132 and the 3rd cryogen chiller 163 between the first degassing mutually the first degassing phase logistics import and the degassing phase logistics just that are connected of logistics pipeline export; The debutylize unit comprises debutanizing tower 61 and overhead condenser 62, is provided with between debutanizing tower 61 and the depropanizing tower 51 just to take off the liquid phase stream pipeline; Overhead condenser 62 has the import and the cooling that are connected with the tower top outlet of debutanizing tower 61 and coagulates the effusive outlet of after product.
Separation preferably for gases such as the oil gas that satisfies complicated component, oil refinery dry gas, methanol-to-olefins product gas, in above-mentioned olefin separation system, be provided with depropanizing unit and debutylize unit, utilize depropanizing tower 51 that four hydro carbons of the carbon in the gas to be separated and carbon four above hydro carbons and carbon three hydro carbons and carbon three following hydro carbons are separated and form the first degassing logistics and contain carbon four hydro carbons and the first liquid phase stream that takes off of carbon four above hydro carbons mutually that contains carbon three hydro carbons and carbon three following hydro carbons.First degassing phase logistics wherein enters above-mentioned demethanizing unit and carries out separating treatment, and, before degassing phase logistics is just entering just demethanizing tower 11 successively in first ice chest 141 with the demethanizing tower 11 isolated first gaseous stream heat exchange just, in the 3rd cryogen chiller 163 with after the cryogen heat exchange, lowered the temperature significantly, therefore, reduced the energy consumption that first demethanizing tower 11 carries out low temperature separation process.Wherein first takes off liquid phase stream and enters debutanizing tower 61 and separate and obtain carbon four-product and carbon five products, realized fully careful separation of unstripped gas is helped the utilization of unstripped gas.
According to another kind of typical embodiment of the present utility model, also providing a kind of utilizes above-mentioned olefin separation system to carry out the isolating method of alkene, this alkene separation method comprises that separating main component is hydrogen, the process of the gas mixture of carbon three hydro carbons and carbon three following hydro carbons, this process comprises demethanizing process just, membrane sepn process and time demethanizing process, make gas mixture just carry out first gaseous stream and first liquid phase stream that non-clear cutting obtains being separated from each other in the demethanizing process, first gaseous stream comprises hydrogen, methane and C2 hydrocarbon class, first liquid phase stream comprise C2 hydrocarbon class and carbon three hydro carbons; Make first gaseous stream carry out rich hydrocarbon stream and hydrogen rich stream that membrane sepn obtains being separated from each other; Make rich hydrocarbon stream in inferior demethanizing process, carry out clear cut second gaseous stream and second liquid phase stream.
Above-mentioned alkene separation method adopts non-clear cutting method to substitute clear cutting method commonly used at present at the cat head place of first demethanizing tower 11, has reduced cold load and thermal load required in the first demethanizing sepn process and has promptly reduced energy consumption.With first demethanizing tower 11 and time demethanizing tower 17 is that example illustrates above-mentioned alkene separation method, so-called non-clear cutting is that the content to the C2 hydrocarbon class of the cat head component of first demethanizing tower 11 does not need to reach below 5% of clear cutting, but it is a part of C2 hydrocarbon class of first demethanizing tower 11 is separated as first gaseous stream with the light constituent of cat head, and another part C2 hydrocarbon class and carbon three hydro carbons are separated at the bottom of the tower as first liquid phase stream, do not contain carbon three and carbon three above hydro carbons like this in tower first gaseous stream, thereby the volume of carbon three hydro carbons of loss accounts for below 0.01% of carbon three cumulative volumes in first demethanizing tower 11, the temperature and pressure that those skilled in the art can select suitable non-clear cutting according to the tolerable temperature and the pressure of device.The membrane separation process that above-mentioned alkene separation method adopts obtains rich hydrocarbon stream and hydrogen rich stream with the hydrogen of the hydro carbons in first gaseous stream effective the separation, wherein can be used for the separatory membrane that separatory membrane of the present utility model includes but not limited to polyetherimide material.CH in the isolated rich hydrocarbon stream of membrane separation process
4/ H
2Molecule ratio is bigger, and then has increased inferior demethanizing tower 17 CH of cat head place
4Dividing potential drop, therefore only the temperature of inferior demethanizing tower 17 need be reduced to higher dew point and can isolate CH
4And H
2, the required energy consumption of cooling has reduced in sepn process so; And, owing to having only few in feasible time isolating second gaseous stream of demethanizing tower 17 cats head of increasing of dew point or even not having ethene, there are not hydrogen and methane in second liquid phase stream, therefore reduced the loss of ethene; Simultaneously, the realization of above-mentioned technique effect can significantly reduce the isolating investment of alkene.
In the another kind of preferred embodiment of the utility model, contain volume percent in first gaseous stream that first demethanizing process obtains and be 15 ~ 90% C2 hydrocarbon class; The volume percent of hydrogen is 75～95% in the hydrogen rich stream that the membrane sepn process obtains, and the volume of hydrogen accounts for 45～65% of hydrogen cumulative volume in first gaseous stream in the hydrogen rich stream; Volume content≤2% of ethene in second gaseous stream that inferior demethanizing process obtains.By pressure and temperature being controlled the result of non-clear cutting, membrane sepn and the clear cutting that can obtain envisioning, help the control of the product that whole alkene separation method obtains.
In order rationally to use heat and the cold that is produced in the sepn process, above-mentioned separation main component is that the process of the gas mixture of hydrogen, carbon three hydro carbons and carbon three following hydro carbons also comprises and makes gas mixture successively through carrying out heat exchange, carry out carrying out first demethanizing process after the heat exchange with cryogen with first gaseous stream that is obtained by non-clear cutting; Make rich hydrocarbon stream successively through processed compressed, with by isolated first gaseous stream of first demethanizing process carry out heat exchange, with by isolated second liquid phase stream of inferior demethanizing process carry out heat exchange, with carry out the laggard places demethanizing of heat exchange process by isolated second gaseous stream of inferior demethanizing process; Make by isolated second gaseous stream of inferior demethanizing and rich hydrocarbon stream and carry out the cooling of expanding before the heat exchange; Make part first liquid phase stream repeat described demethanizing process just after reheat seethes with excitement by first demethanizing separation.
In olefin separation process, first gaseous stream that gas mixture to be separated and the first isolated temperature of demethanizing process is lower carries out heat exchange, rich hydrocarbon stream and the first gas phase thing, the second liquid phase thing and second gaseous stream and carries out heat exchange, all be to utilize the heat exchange that the difference of heat is carried out in the separating step in the sepn process, therefore can reduce the input of external heat-eliminating medium, save separation costs.
In another preferred embodiment of the utility model, above-mentioned alkene separation method comprises that also making unstripped gas to be separated carry out depropanizing handles the back compression to form gas mixture; Make part first liquid phase stream carry out the deethanizing processing and obtain deethanizer overhead stream and the 3rd liquid phase stream; Make deethanizer overhead stream and hydrogen rich stream and/or external hydrogen carry out hydrogenation acetylene removal reaction and obtain the mixture of ethylene that contains after the acetylene removal, will contain mixture of ethylene rectifying again and obtain ethylene product; The 3rd liquid phase stream rectifying is obtained the 4th gaseous stream and the logistics mutually of the 4th liquid phase, make the 4th gaseous stream and the part first liquid phase stream heat exchange after the further removal of impurity is handled and form propylene product; After making the 4th liquid phase stream and second gaseous stream carry out heat exchange, the 4th liquid phase stream after a part of heat exchange and cryogen are further carried out heat exchange be used for absorbing ethene in the gaseous substance that first demethanizing process desire forms described first gaseous stream, the 4th liquid phase stream after another part heat exchange is carried as combustion gas.It is in order to obtain the gas mixture of suitable separation temperature that unstripped gas to be separated is carried out recompressing after depropanizing is handled, because separation temperature rises along with pressure and raises, therefore raw gas pressure infinitely can not be raise, otherwise energy consumption also sharply raises thereupon, so between general exert pressure to 2.0～4.0MPA with gas mixture.
Can be used for unstripped gas to be separated of the present utility model and include but not limited to oil gas, oil refinery dry gas, methanol-to-olefins product gas, the utilization sources of hydrogen that isolated hydrogen rich stream reacts as acetylene hydrogenation from unstripped gas, reduce the consumption of external hydrogen, saved the synthetic cost of ethene.And, not carbon containing three and carbon three above hydro carbons in first gaseous stream that the non-clear cutting of demethanizing process just forms, therefore having only first liquid phase stream need carry out the deethanizing processing gets final product, make energy consumption and load that deethanizing is handled to reduce, and then the investment and the running cost of deethanizing device can correspondingly be reduced.
The above is a preferred embodiment of the present utility model only, is not limited to the utility model, and for a person skilled in the art, the utility model can have various changes and variation.All within spirit of the present utility model and principle, any modification of being done, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
Claims (8)
1. olefin separation system, described olefin separation system comprises the demethanizing unit, it is characterized in that, described demethanizing unit comprises just demethanizing tower (11), membrane separation assemblies (12) and inferior demethanizing tower (17),
Be provided with the first gaseous stream pipeline between the tower top outlet of described demethanizing tower (11) just and the import of described membrane separation assemblies (12);
Be provided with rich hydrocarbon stream pipeline between the rich hydrocarbon stream outlet of described membrane separation assemblies (12) and the import of described demethanizing tower (17).
2. olefin separation system according to claim 1, it is characterized in that, described demethanizing unit also comprises first compressor (131), first ice chest (141), first interchanger (151), second interchanger (152), the first cryogen chiller (161) and decompressor (18)
Has the second gaseous stream pipeline between the import of the tower top outlet of described demethanizing tower (17) and described decompressor (18);
Described first compressor (131) is arranged on the described rich hydrocarbon stream pipeline;
Described first ice chest (141) has:
Stream in first gaseous stream, first ice chest is serially connected in the described first gaseous stream pipeline;
Stream in rich hydrocarbon stream first ice chest is serially connected in the rich hydrocarbon stream pipeline between the import of described first compressor (131) and described demethanizing tower (17);
Described first interchanger (151) has:
Stream in rich hydrocarbon stream first interchanger is serially connected in the described rich hydrocarbon stream pipeline between the import of stream and described demethanizing tower (17) in described rich hydrocarbon stream first ice chest;
Stream in second liquid phase stream, first interchanger is connected with the tower bottom outlet of described demethanizing tower (17), and described rich hydrocarbon stream and described second liquid phase stream carry out heat exchange in described first interchanger (151); Described second interchanger (152) has:
Stream in rich hydrocarbon stream second interchanger is serially connected in the described rich hydrocarbon stream pipeline between the import of stream and described demethanizing tower (17) in rich hydrocarbon stream first interchanger;
Stream in second gaseous stream, second interchanger is connected with the outlet of described decompressor (18), and described rich hydrocarbon stream and described second gaseous stream carry out heat exchange in described second interchanger (152);
The described first cryogen chiller (161) is arranged between the import of interior stream of described rich hydrocarbon stream second interchanger and described demethanizing tower (17).
3. olefin separation system according to claim 2 is characterized in that, described demethanizing unit also comprises:
First reboiler (191), formation first circulation line is connected with the first tower bottom outlet of described demethanizing tower (11) just and links to each other with the described tower still of demethanizing tower (11) just;
Second reboiler (192), formation second circulation line is connected with the second tower bottom outlet of described demethanizing tower (11) just and links to each other with the described tower still of demethanizing tower (11) just.
4. olefin separation system according to claim 3 is characterized in that described olefin separation system also comprises the ethylene distillation unit, and described ethylene distillation unit comprises:
Hydrogenation acetylene removal reactor (21) has:
The hydrogen gas stream import, and have the hydrogen rich stream pipeline between the outlet of the hydrogen rich stream of described membrane separation assemblies (12);
The hydrocarbon material import, and have the second liquid phase stream pipeline between the tower bottom outlet of described demethanizing tower (17);
The ethylene product outlet;
Ethylene rectification tower (22) is connected with described ethylene product outlet.
5. olefin separation system according to claim 4 is characterized in that, described olefin separation system also comprises deethanizing unit and propylene rectification cell,
Described deethanizing unit comprises deethanizing column (31), and described deethanizing column (31) has:
The first liquid phase stream import, and have the first liquid phase stream pipeline between the 3rd tower bottom outlet of described demethanizing tower (11) just;
The deethanizer overhead stream outlet, and have hydro carbons acetylene removal mass transport pipeline between the hydrocarbon material import of described hydrogenation acetylene removal reactor (21);
Described propylene rectification cell comprises:
Propylene rectification tower (41) has:
The 3rd liquid phase stream import, and have the 3rd liquid phase stream pipeline between the tower bottom outlet of described deethanizing column (31);
The outlet of cat head propylene;
Return tank of top of the tower (42), be connected with the outlet of the cat head propylene of described propylene rectification tower (41) and constitute the 3rd circulation line with described propylene rectification tower (41), described first reboiler (191) or second reboiler (192) have propylene import and the propylene outlet that is connected with described the 3rd circulation line.
6. olefin separation system according to claim 5, it is characterized in that, also be provided with control valve (43) on described the 3rd circulation line between described propylene rectification tower (41) and the described return tank of top of the tower (42), described control valve (43) is arranged in parallel with described first reboiler (191) or second reboiler (192).
7. olefin separation system according to claim 5 is characterized in that, described olefin separation system also comprises second ice chest (142),
Described second ice chest (142) has the second gas phase liquid and flows stream in second ice chest, and the described second gas phase liquid flows the interior stream of second ice chest and is connected with the interior stream of second gaseous stream, second interchanger of described second interchanger (152);
Have two article of the 4th liquid phase stream pipeline between described propylene rectification tower (41) and described second ice chest (142),
One article of the 4th liquid phase stream pipeline wherein passes described second ice chest (142) back and is connected with gas ductwork;
Another article the 4th liquid phase stream pipeline passes to extend to behind described second ice chest (142) with described demethanizing tower (11) just and is connected, described olefin separation system also comprises the second cryogen chiller (162), and the described second cryogen chiller (162) is arranged on described second ice chest (142) and described the 4th liquid phase stream pipeline between the demethanizing tower (11) just.
8. olefin separation system according to claim 7 is characterized in that, described olefin separation system also comprises: the depropanizing unit comprises:
Depropanizing tower (51), the tower top outlet of described depropanizing tower (51) and the described logistics pipeline mutually of the degassing just that just is provided with between the demethanizing tower (11);
Moisture eliminator (52) is connected with the import of described depropanizing tower (51) and carries unstripped gas to be separated to described depropanizing tower (51);
Second compressor (132) is arranged on the described degassing just between described depropanizing tower (51) and the described demethanizing tower (11) just mutually on the logistics pipeline;
The 3rd cryogen chiller (163), be arranged on the described degassing just between described second compressor (132) and the described demethanizing tower (11) just mutually on the logistics pipeline, described first ice chest (141) have with described second compressor (132) and described the 3rd cryogen chiller (163) between the described degassing just mutually the first degassing phase logistics import and the degassing phase logistics just that are connected of logistics pipeline export;
The debutylize unit comprises:
Debutanizing tower (61), and be provided with the first liquid phase stream pipeline that takes off between the described depropanizing tower (51);
Overhead condenser (62) has the import and the cooling that are connected with the tower top outlet of described debutanizing tower (61) and coagulates the effusive outlet of after product.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320045987XU CN203079876U (en) | 2013-01-28 | 2013-01-28 | Olefin separation system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320045987XU CN203079876U (en) | 2013-01-28 | 2013-01-28 | Olefin separation system |
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| CN203079876U true CN203079876U (en) | 2013-07-24 |
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