CN107285981B - Demethanizer heat exchange system and heat exchange method - Google Patents
Demethanizer heat exchange system and heat exchange method Download PDFInfo
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- CN107285981B CN107285981B CN201610201050.5A CN201610201050A CN107285981B CN 107285981 B CN107285981 B CN 107285981B CN 201610201050 A CN201610201050 A CN 201610201050A CN 107285981 B CN107285981 B CN 107285981B
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Abstract
The invention discloses a demethanizer heat exchange system and a demethanizer heat exchange method. The heat exchange system adopts one of the following three modes: an outlet pipeline at the bottom of the A1 # hydrogen-methane separation tank is divided into a demethanizer or a demethanizer reflux tank; b, arranging a postcooler on the top of the reflux tank of the demethanizer, and connecting a branch of outlet pipeline at the bottom of the 1# hydrogen-methane separation tank with the postcooler and then with the reflux tank of the demethanizer; and a gas-liquid separation tank is arranged behind the cold box C, a gas phase outlet of the demethanizer reflux tank is connected with the cold box and then connected with the gas-liquid separation tank, and the bottom of the gas-liquid separation tank is connected with the demethanizer reflux tank. The invention reasonably optimizes the self refrigeration quantity matching of deep cooling without changing the refrigerant level and the outlet pressure of the compressor, utilizes the local abundant refrigeration quantity to cool the gas phase at the top of the reflux tank of the demethanizer, increases the heat transfer temperature difference of the condenser of the demethanizer and reduces the ethylene loss.
Description
Technical Field
The invention relates to the field of ethylene production, in particular to a demethanization heat exchange system and a demethanization heat exchange method.
Background
The ethylene device has the longest flow and the most complex heat exchange network in a chemical device, and is used as a complex system, and the use of heat and cold in the system is accurately matched. Ethylene separation can be divided into several zones, quench, compression, cold zone, hot zone, refrigeration and utilities. The demethanizer in the cold section, which achieves separation of ethylene from methane hydrogen under conditions that meet stringent ethylene loss rates, is one of the cores of the overall separation plant.
The ethane is used as a high-quality raw material with high conversion rate and good selectivity for steam cracking, and compared with other ethylene raw materials, the steam cracking reaction product of the ethane has relatively low methane content and relatively high hydrogen content, so that the separation difficulty is increased, and higher requirements are provided for cold zone separation.
The refrigerant of the demethanizer is provided by a refrigeration system, and because the boiling point of hydrogen is lower, the liquefaction is more difficult, more hydrogen is condensed, a refrigerant with a cooler stage is needed, the realization of changing the stage of the refrigerant is difficult under the condition that the refrigerant proportion is not changed, and as a result, the heat transfer temperature difference of the condenser of the demethanizer is too low (lower than 2.5 ℃), the loss rate of ethylene is increased, namely the cold cannot be cooled down. Ethylene loss can only be controlled by increasing the exit pressure of the cracked gas compressor to increase the operating pressure of the demethanizer, but this greatly increases the compressor power consumption, resulting in increased overall system energy consumption. On the other hand, the recovery of cold energy of tail gas in the cold phase may be unbalanced locally, which causes the local temperature of the cracked gas to be too low, i.e. "the cracked gas is not cooled down", so that the temperature of the cracked gas is difficult to control, which affects the gas-liquid load distribution in the tower and causes the efficiency loss of the tray. The tail gas cold recovery is insufficient, the tail gas cold recovery enters a subsequent flow, and the cold temperature level is not matched with the process logistics, so that waste is caused, and the tail gas cold recovery is difficult to control.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a demethanizer heat exchange system and a demethanizer heat exchange method. The invention reasonably optimizes the self refrigeration quantity matching of deep cooling without changing the refrigerant level and the outlet pressure of the compressor, utilizes the local abundant refrigeration quantity to cool the gas phase at the top of the reflux tank of the demethanizer, increases the heat transfer temperature difference of the condenser of the demethanizer and reduces the ethylene loss.
One of the objects of the present invention is to provide a heat exchange system for a demethanizer, comprising: the device comprises a demethanizer, a demethanizer condenser, a demethanizer reflux tank, a No. 1 hydrogen-methane knockout tank, a No. 2 hydrogen-methane knockout tank and a cold box, wherein the cold box comprises a No. 1 cold box, a No. 2 cold box, a No. 3 cold box and a No. 4 cold box which are sequentially connected, an outlet at the top of the demethanizer is connected with the demethanizer condenser and then connected with the demethanizer reflux tank, a gas phase outlet of the demethanizer reflux tank is connected with the No. 2 cold box, a liquid phase outlet of the demethanizer reflux tank is connected with the upper part of the demethanizer, the No. 2 cold box is connected with the No. 1 hydrogen-methane knockout tank, the No. 2,
the heat exchange system adopts one of the following three modes:
an outlet pipeline at the bottom of the A1 # hydrogen-methane separation tank is divided into a demethanizer or a demethanizer reflux tank;
a back cooler is arranged on the top of the reflux tank of the demethanizer B, and a branch of outlet pipeline at the bottom of the 1# hydrogen-methane separation tank is connected with the back cooler and then connected with the reflux tank of the demethanizer; the gas phase outlet of the demethanizer reflux tank is connected with the aftercooler and then connected with the No. 2 cold box;
and a gas-liquid separation tank is arranged behind the cold box C, a gas phase outlet of the demethanizer reflux tank is connected with the cold box and then connected with the gas-liquid separation tank, and the bottom of the gas-liquid separation tank is connected with the demethanizer reflux tank.
The second purpose of the invention is to provide a heat exchange method adopting the heat exchange system. The method comprises the following steps: the loss of ethylene is reduced by lowering the temperature of the demethanizer tail gas.
Specifically, one of the following three methods can be adopted:
the method comprises the following steps:
and (3) introducing a liquid phase from the No. 1 hydrogen-methane separation tank to the demethanizer directly to reduce the temperature of the gas phase at the top of the demethanizer, or sending the liquid phase to the reflux tank of the demethanizer, reducing the temperature of the reflux tank of the demethanizer, and returning the liquid phase at the bottom of the tank to the top of the demethanizer, so that the temperature of the gas phase at the top of the demethanizer is reduced.
The second method comprises the following steps:
and (3) introducing a liquid phase from the No. 1 hydrogen-methane separation tank to directly send to the aftercooler, cooling the gas phase at the top of the reflux tank of the demethanizer by the aftercooler, returning the liquid phase material flow of the aftercooler to the reflux tank of the demethanizer, reducing the temperature of the reflux tank of the demethanizer, and returning the liquid phase at the bottom of the tank to the top of the demethanizer so as to reduce the temperature of the gas phase at the top of the demethanizer.
The demethanizer aftercooler means that after the gas phase at the top of the demethanizer is condensed by a demethanizer condenser, gas-liquid separation is realized in a reflux tank, the gas phase is further cooled by the demethanizer aftercooler, the liquid phase returns to the reflux tank, and the gas phase is sent to a fuel gas system after being used as tail gas to utilize cold quantity.
The third method comprises the following steps:
the gas phase at the top of the reflux tank of the demethanizer is sent to a cooling box for cooling, and then gas-liquid separation is realized in a gas-liquid separation tank; the liquid phase returns to the reflux tank of the demethanizer, the temperature of the reflux tank of the demethanizer is reduced, and the liquid phase at the bottom of the tank returns to the top of the demethanizer, so that the temperature of the gas phase at the top of the demethanizer is reduced.
The demethanizer reflux drum overhead vapor phase is preferably sent to a # 3 cold box for cooling.
The third method can fully utilize the cold energy of the system, and achieve the purposes of reducing the temperature of the tail gas, reducing the loss of ethylene, optimizing the heat exchange network and saving the consumption of the refrigerant.
The invention can be realized in the following way:
in the first scheme, a liquid phase is introduced from a No. 1 hydrogen methane separating tank and is directly sent to a demethanizer (or a demethanizer reflux tank) to be used as reflux;
a demethanizer aftercooler is additionally arranged in the scheme II, the demethanizer methane tail gas is cooled, and the liquid phase of the 1# hydrogen-methane separation tank is used as a refrigeration medium;
and in the third scheme, the demethanizer aftercooler is arranged at a proper position of the cold box sequence (preferably behind the 3# cold box), the gas phase at the top of the demethanizer reflux tank obtains cold energy from the cold box for cold energy recovery, and the cold energy can be recovered to the maximum extent if the temperature is reasonably matched.
The heat exchange method can comprise the following steps:
the first scheme is as follows:
(1) introducing a liquid phase from a No. 1 hydrogen-methane separation tank;
(2) the liquid phase is directly sent to the top of the demethanizer for reflux;
(3) or the liquid phase is sent to a demethanizer reflux drum or other line, indirectly as demethanizer reflux. The self-flow can be directly realized by pressure difference, and the low-temperature pump can be used for pressurization under special conditions.
Scheme II:
(1) the top of the reflux tank of the demethanizer is additionally provided with an after-cooler;
(2) cooling the gas phase on the reflux tank of the demethanizer by a postcooler, then carrying out the subsequent flow of the gas phase, and returning the condensed liquid phase to the reflux tank of the demethanizer;
(3) introducing a liquid phase from the 1# hydrogen-methane separation tank as a refrigerant of an after-cooler;
(4) the cold agent enters the position matched with the temperature level of the subsequent cold box after being used.
The third scheme is as follows:
(1) recovering tail gas cold energy from the gas phase at the top of the reflux tank of the demethanizer in a No. 3 cold box, and cooling the tail gas by the gas phase;
(2) and the cooled gas phase at the top of the tower enters a gas-liquid separation tank of a post-cooler of the demethanizer, the gas phase continues to enter the subsequent flow, and the liquid phase returns to a reflux tank of the demethanizer.
The invention can select one or a combination of a plurality of schemes according to local conditions in consideration of the implementation difficulty and feasibility of the modification of the existing device.
Under the conditions of not changing the refrigerant level and not changing the outlet pressure of a cracking gas compressor, the cold quantity matching of a cold area is reasonably optimized, the locally abundant cold quantity in the system is adopted, the abundant cold quantity can be sourced from a hydrogen-methane separating tank, a cold box for recovering the cold quantity of tail gas or other positions, the material flow directly enters a demethanizer reflux tank or indirectly transfers heat with the gas at the top of the demethanizer reflux tank for cooling, the gas phase still enters a subsequent flow, the condensed liquid phase returns to the demethanizer reflux tank, the temperature of the demethanizer reflux tank is reduced, the temperature at the top of the demethanizer is further reduced, the heat transfer temperature difference of a demethanizer condenser is improved, and the ethylene loss of the demethanizer is reduced.
Drawings
FIG. 1 is a schematic diagram of the demethanizer heat exchange system of example 1
FIG. 2 is a schematic diagram of the demethanizer heat exchange system of example 2
FIG. 3 is a schematic diagram of the demethanizer heat exchange system of example 3
FIG. 4 is a schematic diagram of a demethanizer heat exchange system of the prior art
Description of reference numerals:
equipment bit number:
DA-301: demethanizer, DA-302 carbon two scrub column
D-301: demethanizer first feed knockout drum, D-302: a second feed knockout drum of the demethanizer,
D-303X: 1# Hydrogen-methane separation tank, D-304X: 2# Hydrogen methane knockout drum, D-305 XN: vapor-liquid separation tank, E-301X: 1# cold box, E-302X: 2# cold box, E-303X: 3# cold box, E-304X: 4# cold box, E-311: demethanizer condenser, E-312: demethanizer reboiler, E-313N: aftercooler, KX-301: a methane tail gas expansion machine,
stream number:
1: 1# demethanizer feed, 2: 2# demethanizer feed, 3: the feed to the 3# demethanizer,
4: demethanizer overhead, 5: cooled demethanizer overhead, 6: the methane tail gas at the top of the tank is refluxed,
7: the reflux of the demethanizer is carried out,
11N: 1# Hydrogen-methane knockout drum liquid phase demethanizer reflux drum, 12N: 1# Hydrogen methane knockout drum liquid phase goes demethanizer aftercooler, 13N: and (3) returning the refrigerant side of the post-cooler of the demethanizer to the cold box for recovering cold energy, wherein the refrigerant side of the post-cooler of the demethanizer is 14N: returning the condensate phase of the aftercooler to a reflux tank of the demethanizer, and carrying out 15N: the demethanizer tail gas cooled by E-303X goes to a gas-liquid separation tank, 16N: liquid phase of the gas-liquid separation tank, 17N: gas phase of gas-liquid separation tank
20: tail gas
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
As shown in fig. 1, a heat exchange system of a demethanizer.
The method comprises the following steps: the system comprises a demethanizer DA-301, a demethanizer condenser E-311, a demethanizer reflux tank D-305, a 1# hydrogen-methane knockout tank D-303X, a 2# hydrogen-methane knockout tank D-304X and a cold box, wherein the cold box comprises a 1# cold box E-301X, a 2# cold box E-302X, a 3# cold box E-303X and a 4# cold box E-304X which are sequentially connected, an outlet at the top of the demethanizer DA-301 is connected with the demethanizer condenser E-311 and then connected with the demethanizer reflux tank D-305, a gas phase outlet of the demethanizer reflux tank D-305 is connected with the 2# cold box E-302X, a liquid phase outlet of the demethanizer reflux tank D-305 is connected with the upper part of the demethanizer DA-301, the 2# cold box E-302X is connected with the 1# hydrogen-methane knockout tank D-303X, and the 2# hydrogen-methane knockout tank D-304X is connected with the 1# cold, the outlet pipeline at the bottom of the 1# hydrogen methane separating tank D-303X is branched off and connected with a demethanizer reflux tank D-305.
And introducing a liquid phase 11N from the 1# hydrogen-methane separation tank, directly sending the liquid phase to a reflux tank of the demethanizer, and indirectly serving as reflux. The self-flow can be directly realized by pressure difference, and the liquid can be pressurized by using a cryogenic pump under special conditions.
Because the temperature of the liquid phase 11N of the 1# hydrogen-methane separation tank is far lower than that of the reflux tank of the demethanizer, the temperature of the reflux tank is reduced under the condition that the liquid in the reflux tank is fully mixed. On one hand, the reduction of the temperature of the reflux tank reduces the reflux temperature of the demethanizer, so that the temperature of the gas phase at the top of the demethanizer is reduced, the heat transfer temperature difference of a condenser E-311 of the demethanizer is increased, and the heat transfer effect of the condenser of the demethanizer is improved; on the other hand, the liquid phase temperature of the reflux tank is reduced, so that the gas phase temperature is reduced, and the ethylene loss of the tail gas 6 of the demethanizer is reduced.
Example 2
As shown in figure 2 of the drawings, in which,
a demethanizer heat exchange system.
The method comprises the following steps: a demethanizer DA-301, a demethanizer condenser E-311, a demethanizer reflux tank D-305, a 1# hydrogen methane knockout tank D-303X, a 2# hydrogen methane knockout tank D-304X and a cold box, the cold box comprises a 1# cold box E-301X, a 2# cold box E-302X, a 3# cold box E-303X and a 4# cold box E-304X which are sequentially connected, an outlet at the top of the demethanizer DA-301 is connected with a demethanizer condenser E-311 and then connected with a demethanizer reflux tank D-305, a gas phase outlet of the demethanizer reflux tank D-305 is connected with the 2# cold box E-302X, a liquid phase outlet of the demethanizer reflux tank D-305 is connected with the upper part of the demethanizer DA-301, the 2# cold box E-302X is connected with a 1# hydrogen methane separation tank D-303X, and the 2# hydrogen methane separation tank D-304X is connected with the 1# cold box E-301X.
An outlet pipeline at the bottom of the 1# hydrogen-methane separation tank D-303X is divided into a branch which is connected with the after cooler E-313N and then connected with the demethanizer reflux tank D-305; and a gas phase outlet of the demethanizer reflux tank D-305 is connected with an aftercooler E-313 and then connected with a # 2 cold box E-302X.
The demethanizer reflux drum overhead gas is first cooled in E-313X, the gas phase goes to the expander, and the liquid phase 14N is returned to the reflux drum. A liquid phase 12N to E-313X is divided from the 1# hydrogen methane separation tank to be used as a refrigerant, and after the refrigerant is used, the liquid phase 13N is returned to a proper position, such as between E-303X and E-304X.
The after cooler E-313X cools the gas phase 6 at the top of the reflux tank of the demethanizer, and the liquid phase material flow 14N returns to the reflux tank of the demethanizer to reduce the temperature of the reflux 7, so that the gas phase temperature at the top of the demethanizer is reduced, the heat transfer temperature difference of a condenser E-311 of the demethanizer is increased, and the heat transfer effect of the condenser of the demethanizer is improved; the gas phase temperature is reduced, and the ethylene loss of the tail gas of the demethanizer is reduced.
Compared with the embodiment 2, the embodiment 1 has a simple mode and no additional equipment, more methane hydrogen tail gas enters the expander, more cooling capacity is provided for E-302X, but the increase of the low-pressure tail gas quantity can enter fuel gas only by further pressurizing in the subsequent flow, and the power consumption of the subsequent compressor can be increased.
Example 3
As shown in fig. 3, a demethanizer heat exchange system.
The method comprises the following steps: the system comprises a demethanizer DA-301, a demethanizer condenser E-311, a demethanizer reflux tank D-305, a 1# hydrogen-methane knockout tank D-303X, a 2# hydrogen-methane knockout tank D-304X and a cold box, wherein the cold box comprises a 1# cold box E-301X, a 2# cold box E-302X, a 3# cold box E-303X and a 4# cold box E-304X which are sequentially connected, an outlet at the top of the demethanizer DA-301 is connected with the demethanizer condenser E-311 and then connected with the demethanizer reflux tank D-305, a gas phase outlet of the demethanizer reflux tank D-305 is connected with the 2# cold box E-302X, a liquid phase outlet of the demethanizer reflux tank D-305 is connected with the upper part of the demethanizer DA-301, the 2# cold box E-302X is connected with the 1# hydrogen-methane knockout tank D-303X, and the 2# hydrogen-methane knockout tank D-304X is connected with the 1# cold,
and a gas-liquid separation tank D-305XN is arranged behind the 3# cold box E-303X, a gas-phase outlet of the demethanizer reflux tank D-305 is connected with the 3# cold box E-303X and then connected with the gas-liquid separation tank D-305XN, and the bottom of the gas-liquid separation tank D-305XN is connected with the demethanizer reflux tank D-305.
In this embodiment, the third cold box E-303X is actually used as an aftercooler, and the gas phase 6 at the top of the reflux tank of the demethanizer is sent to the third cold box E-303X for cooling, and then gas-liquid separation is realized in the gas-liquid separation tank. The liquid phase 16N returns to the reflux tank, and the gas phase 17N continues to the subsequent flow.
The liquid phase material flow 16N returns to the reflux tank of the demethanizer to reduce the temperature of the reflux 7, further reduce the temperature of the gas phase 4 at the top of the demethanizer, increase the heat transfer temperature difference of the condenser E-311 of the demethanizer and improve the heat transfer effect of the condenser of the demethanizer; the gas phase temperature is reduced, and the ethylene loss at the top of the demethanizer can be reduced. Compared with the two schemes of the embodiments 1 and 2, the scheme has modification on part of the flow of the cold box for recovering the cold, if the scheme is implemented in the modification of the existing device, the scheme is limited by the cold box, but the scheme can be difficult to implement in the existing device, and the cold can be recovered to the maximum extent by utilizing the cold at the position because the temperature of the top of the demethanizer is matched with the temperature of E-303X.
The components in the tail gas of each example are shown in table 1, and it can be seen that, under the condition that the refrigerant level and the cracked gas pressure are not changed, the temperature of the tail gas can be effectively reduced by adopting the scheme of the invention, so that the ethylene loss (low ethylene content) is reduced, the example 1 is simple and convenient to implement, the technical modification of the interior of a plant can be completed, the ethylene loss of the example 2 is less than that of the example 1, the method can be implemented in the modification of a device, and the effect of the example 3 is optimal, but needs to be comprehensively considered at the beginning of the design.
TABLE 1
| Tail gas | Initial | Example 1 | Example 2 | Example 3 |
| Phase state | Gas phase | Gas phase | Gas phase | Gas phase |
| Temperature of | -98.23 | -98.19 | -98.34 | -98.52 |
| Pressure kPaG | 3055.00 | 3055.00 | 3038.00 | 3038.00 |
| Mol% of | ||||
| Hydrogen gas | 6.8302 | 6.5550 | 6.8284 | 6.8295 |
| Carbon monoxide | 0.1817 | 0.1910 | 0.1818 | 0.1818 |
| Methane | 92.8880 | 93.1979 | 92.9437 | 92.9565 |
| Acetylene | 0.0000 | 0.0000 | 0.0000 | 0.0000 |
| Ethylene | 0.1000 | 0.0560 | 0.0461 | 0.0322 |
| Ethane (III) | 0.0001 | 0.0000 | 0.0000 | 0.0000 |
Claims (2)
1. A demethanizer heat exchange system comprising: demethanizer, demethanizer condenser, demethanizer reflux tank, 1# hydrogen methane knockout drum, 2# hydrogen methane knockout drum and cold box, the cold box is including the 1# cold box, 2# cold box, 3# cold box and the 4# cold box that connect gradually, and demethanizer top exit linkage demethanizer condenser back connects demethanizer reflux tank, and demethanizer reflux tank gas phase exit linkage 2# cold box, demethanizer reflux tank liquid phase exit linkage demethanizer upper portion, 1# hydrogen methane knockout drum is connected to 2# cold box, and 1# cold box, its characterized in that are connected to 2# hydrogen methane knockout drum:
the heat exchange system adopts one of the following three modes:
an outlet pipeline at the bottom of the A1 # hydrogen-methane separation tank is divided into a demethanizer or a demethanizer reflux tank;
b, a back cooler is arranged on the top of the reflux tank of the demethanizer, an outlet pipeline at the bottom of the 1# hydrogen-methane separation tank is divided into a branch which is connected with the back cooler and then connected with the reflux tank of the demethanizer, a refrigerant outlet of the back cooler is connected with a position matched with the temperature level of a subsequent cold box, and a gas phase outlet of the reflux tank of the demethanizer is connected with the back cooler and then connected with the 2# cold box;
and a gas-liquid separation tank is arranged behind the C3 # cold box, a gas phase outlet of the demethanizer reflux tank is connected with the 3# cold box and then connected with the gas-liquid separation tank, and the bottom of the gas-liquid separation tank is connected with the demethanizer reflux tank.
2. A method of heat exchange using the demethanizer heat exchange system of claim 1, comprising:
reducing ethylene loss by lowering the temperature of the demethanizer tail gas;
specifically, the method is one of the following three methods:
1) and (3) introducing a liquid phase from the No. 1 hydrogen-methane separation tank to the demethanizer directly to reduce the temperature of the gas phase at the top of the demethanizer, or sending the liquid phase to the reflux tank of the demethanizer, reducing the temperature of the reflux tank of the demethanizer, and returning the liquid phase at the bottom of the tank to the top of the demethanizer, so that the temperature of the gas phase at the top of the demethanizer is reduced.
2) And (3) introducing a liquid phase from the No. 1 hydrogen-methane separation tank to directly send to the aftercooler, cooling the gas phase at the top of the reflux tank of the demethanizer by the aftercooler, returning the liquid phase material flow of the aftercooler to the reflux tank of the demethanizer, reducing the temperature of the reflux tank of the demethanizer, and returning the liquid phase at the bottom of the tank to the top of the demethanizer so as to reduce the temperature of the gas phase at the top of the demethanizer.
3) The gas phase at the top of the reflux tank of the demethanizer is sent to a No. 3 cold box for cooling, and then gas-liquid separation is realized in a gas-liquid separation tank; the liquid phase returns to the reflux tank of the demethanizer, the temperature of the reflux tank of the demethanizer is reduced, and the liquid phase at the bottom of the tank returns to the top of the demethanizer, so that the temperature of the gas phase at the top of the demethanizer is reduced.
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| WO2014064172A2 (en) * | 2012-10-24 | 2014-05-01 | Total Research & Technology Feluy | Process for recovery light molecules from olefinic feedstream |
| CN104870408A (en) * | 2012-12-13 | 2015-08-26 | 道达尔研究技术弗吕公司 | Process for removing light components from an ethylene stream |
| CN104884413A (en) * | 2012-11-15 | 2015-09-02 | 鲁姆斯科技公司 | Recovery of ethylene from methanol to olefins process |
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|---|---|---|---|---|
| WO2014064172A2 (en) * | 2012-10-24 | 2014-05-01 | Total Research & Technology Feluy | Process for recovery light molecules from olefinic feedstream |
| CN104884413A (en) * | 2012-11-15 | 2015-09-02 | 鲁姆斯科技公司 | Recovery of ethylene from methanol to olefins process |
| CN104870408A (en) * | 2012-12-13 | 2015-08-26 | 道达尔研究技术弗吕公司 | Process for removing light components from an ethylene stream |
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