CN103127802A - Cryogenic recovery system and recovery method for ethylene in tail gas - Google Patents
Cryogenic recovery system and recovery method for ethylene in tail gas Download PDFInfo
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- CN103127802A CN103127802A CN2011103856602A CN201110385660A CN103127802A CN 103127802 A CN103127802 A CN 103127802A CN 2011103856602 A CN2011103856602 A CN 2011103856602A CN 201110385660 A CN201110385660 A CN 201110385660A CN 103127802 A CN103127802 A CN 103127802A
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- methane
- absorption tower
- ethene
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 238000011084 recovery Methods 0.000 title claims abstract description 40
- 239000005977 Ethylene Substances 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 176
- 238000010521 absorption reaction Methods 0.000 claims abstract description 70
- 239000007791 liquid phase Substances 0.000 claims abstract description 61
- 238000000926 separation method Methods 0.000 claims abstract description 52
- 239000012071 phase Substances 0.000 claims abstract description 30
- 239000007789 gas Substances 0.000 claims description 71
- 230000005540 biological transmission Effects 0.000 claims description 49
- 229910052739 hydrogen Inorganic materials 0.000 claims description 39
- 239000001257 hydrogen Substances 0.000 claims description 39
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 37
- 239000007788 liquid Substances 0.000 claims description 29
- 238000001816 cooling Methods 0.000 claims description 20
- 239000006227 byproduct Substances 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 9
- 239000007792 gaseous phase Substances 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 239000000047 product Substances 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000010992 reflux Methods 0.000 abstract description 6
- 238000009833 condensation Methods 0.000 description 15
- 230000005494 condensation Effects 0.000 description 15
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a cryogenic recovery system for ethylene in tail gas. The recovery system comprises a methane fractionating tower, methane fractionating tower reflux separation equipment, at least two heat exchange devices and an absorption tower; a discharge port at the top of the methane fractionating tower is communicated with a feed inlet of reflux separation equipment of the methane fractionating tower, a first liquid phase branch of a liquid phase outlet at the bottom of the reflux separation equipment of the methane fractionating tower is sequentially connected with first heat exchange equipment and second heat exchange equipment in series, an inlet at the bottom of the absorption tower is communicated with an outlet of the first heat exchange equipment, a gas phase outlet at the top of the absorption tower is communicated with a gas phase inlet of the second heat exchange equipment, a liquid phase inlet at the top of the absorption tower is communicated with a liquid phase outlet of the second heat exchange equipment, a liquid phase outlet at the bottom of the absorption tower is communicated with an inlet at the bottom of the first heat exchange equipment, and. The invention also relates to a cryogenic recovery method of ethylene in tail gas. The invention improves the recovery rate of ethylene, and the equipment arrangement is simpler and more reasonable, and the energy consumption of the system can not be increased.
Description
Technical field
The present invention relates to the ethylene recovery technical field, be specifically related to cryogenic recovery system and the recovery method of ethene in a kind of tail gas.
Background technology
one of cryogenic separation part main purpose in ethylene production technique is that (general minimum reaching-170 ℃) (is mainly hydrogen with gas-phase feed in plate-fin heat exchanger under certain low temperature range, methane, ethene) after the cooling condensation, heavier rear the continuation condensation and separation of gas phase of liquid phase (being mainly methane and ethene) of separation component in the gas-liquid separation container, separate through multiple condensation, hydrogen the most at last, methane separates with ethene, (main component is methane to obtain hydrogen product and methane hydrogen byproduct, also comprise a small amount of hydrogen), methane hydrogen byproduct provides fuel take the form of self-produced fuel as cracking reaction substantially.
for reducing the content of ethene in tail gas, reduce ethylene loss, existing way is that the gas-liquid separation equipment with separation process changes rectifying column into, reduce ethylene contents in tail gas by rectifying, as shown in Figure 1, through multi-stage condensing, gas-phase feed after separation, enter rectifying column 51 after the 3rd plate-fin heat exchanger 31 is cooling, rectifying column 51 bottom liquid phases are sent into ethylene recovery unit after the 3rd plate-fin heat exchanger 31 reclaims cold, rectifying column 51 top gas are isolated liquid phase part and the gas phase part take methane and hydrogen as main component in gas-liquid separation container 6 after the 4th plate-fin heat exchanger 41 cooling segment condensations, liquid phase part refluxes as rectifying column 51, gas phase part further obtains hydrogen after refrigerated separation and the methane hydrogen byproduct take methane as main component is tail gas, the gas that acts as a fuel uses.It is a part of separating plate-fin heat exchanger used due to overhead condenser, therefore condenser is placed on tower top or higher than the position of tower top, the former schemes synthesis many factors, and tower can not be too high, plate-fin heat exchanger can not be done too greatly, and plate-fin heat exchanger is very large for the Intensity Design impact of tower; Latter's scheme need design a framework higher than tower, considers also uneconomical.At present take supplier as main, therefore for tighter project of duration, restricted many due to the Design and manufacture of plate-fin heat exchanger.In addition, the required cold of top gaseous phase condensation all is taken from the cryogenic separation part, therefore causing cold separating part cold not enough, is the system to the deep cooling with deep cooling Partial Liquid Phase decompression cycles for making up cold not enough institute Adopts measure, increases like this size of total system energy consumption and relevant device.Because cold mainly comes from the cryogenic separation part, the result that causes like this is impossible carry out condensation with lower temperature to the gas phase at top, absorption tower, otherwise the required cold of later separation can't make up, perhaps need strengthen the internal circulating load of system, make up the required cold of system cools, cause larger energy dissipation, offset to a great extent and reclaimed the income that ethene obtains, because internal circulating load increases, equipment investment also will increase.
Summary of the invention
The object of the present invention is to provide the cryogenic recovery system of ethene in a kind of tail gas, on the basis that does not increase system energy consumption, improve Recovery rate of ethylene.
Another object of the present invention is to provide the deep cooling recovery method of ethene in a kind of tail gas.
In order to achieve the above object, the technical solution used in the present invention is:
the cryogenic recovery system of ethene in a kind of tail gas comprises methane fractionating column, methane fractionating column backflow separation equipment, at least two heat transmission equipments and absorption tower, described methane fractionating column top discharge mouth is connected with described methane fractionating column backflow separation equipment charging aperture through heat exchanger, the first liquid phase branch of described methane fractionating column backflow separation equipment bottom liquid phases outlet is connected in series the first heat transmission equipment and the second heat transmission equipment successively, the bottom import of described absorption tower is communicated with described the first heat transmission equipment outlet, the gas phase import of described absorption tower top gaseous phase outlet and described the second heat transmission equipment is communicated with, top, described absorption tower inlet is communicated with the liquid-phase outlet of described the second heat transmission equipment, bottom, described absorption tower liquid-phase outlet is communicated with described the first heat transmission equipment bottom import, described the first heat transmission equipment bottom liquid-phase outlet is communicated with the first inlet of described methane fractionating column.
In such scheme, described absorption tower is plate column, and the number of plates of described plate column is the 3-30 piece.
In such scheme, described absorption tower is packed tower, and the packed height of described packed tower is 0.1～10 meter.
In such scheme, after the first described at least two heat transmission equipment heat-shifts of liquid phase branch's process of described methane fractionating column backflow separation equipment bottom liquid phases outlet, temperature is lower than described absorption tower top gas temperature, and temperature difference is 0 ℃～200 ℃.
In such scheme, after the first described at least two heat transmission equipment heat-shifts of liquid phase branch's process of described methane fractionating column backflow separation equipment bottom liquid phases outlet, temperature is higher than described absorption tower top gas temperature, and temperature difference is 0 ℃～50 ℃.
In such scheme, described at least two heat transmission equipments are plate-fin heat exchanger.
In such scheme, the liquid that top, described absorption tower inlet enters is methane liquid, perhaps hydrogen liquid, perhaps methane and hydrogen mixing material, or methane and hydrogen and ethene mixing material.
In such scheme, described methane fractionating column backflow separation equipment bottom liquid phases outlet is communicated with the second inlet of described methane fractionating column.
In a kind of tail gas, the deep cooling recovery method of ethene, comprise the steps:
The tail gas that (1) will contain ethene absorbs the described cooled tail gas that contains ethene in the absorption tower after the first heat transmission equipment is cooling, isolates the liquid phase part that contains ethene and the gas phase part take methane, hydrogen as main component;
(2) liquid phase part that contains ethene after described separation reclaims cold through the first heat transmission equipment, and the liquid phase after cold recovery is returned to the methane fractionating column, sends into ethylene column after the lower end discharging opening outflow of described methane fractionating column, isolates ethylene product; Simultaneously, after described separation take methane, hydrogen as main gas phase part after the second heat transmission equipment refrigerated separation, isolate hydrogen product and methane hydrogen byproduct;
In described step (1), absorbing absorption liquid used in described absorption tower and be the Partial Liquid Phase that described methane fractionating column top is obtained, to introduce described absorption tower after at least two heat transmission equipments are cooling resulting.
Compare with the prior art scheme, the beneficial effect that the technical solution used in the present invention produces is as follows:
The present invention adopts by drawing one liquid phase as absorption liquid from methane fractionation tower top, this liquid phase cross in plate-fin heat exchanger through at least twice cold after, introduce in the absorption tower ethene in tail gas is absorbed, greatly reduce the content of ethene in tail gas, be that Recovery rate of ethylene improves a lot, and apparatus arrangement advantages of simple more; And twice cooling procedure institute chilling requirement is much smaller through the required cold of segregator condensation with respect to the absorption tower top gaseous phase, and the present invention substantially without impact, can not increase system energy consumption to ice chest system cold balancing.
Description of drawings
Fig. 1 is the structural representation of ethene cryogenic recovery system of the prior art;
The structural representation of the ethene cryogenic recovery system that Fig. 2 provides for the embodiment of the present invention.
The specific embodiment
Below in conjunction with drawings and Examples, technical solution of the present invention is described in detail.
as shown in Figure 2, the embodiment of the present invention provides the cryogenic recovery system of ethene in a kind of tail gas, comprise methane fractionating column 1, methane fractionating column backflow separation equipment 2, the first heat transmission equipment 3, the second heat transmission equipment 4 and absorption tower 5, methane fractionating column 1 top discharge mouth and methane fractionating column backflow separation equipment 2 charging apertures are connected, the 2 bottom liquid phases outlets of methane fractionating column backflow separation equipment are connected in series the first heat transmission equipment 3 and the second heat transmission equipment 4 successively, absorption tower 5 bottom gas phase imports and the first heat transmission equipment 3 gaseous phase outlets are communicated with, the liquid-phase outlet of absorption tower 5 top inlets and the second heat transmission equipment 4 is communicated with, absorption tower 5 bottom liquid-phase outlets and the first heat transmission equipment 3 bottom liquid phase imports are communicated with.
The gas phase import of absorption tower 5 top gaseous phase outlets and the second heat transmission equipment 4 is communicated with.The first inlet of the first heat transmission equipment 3 bottom liquid-phase outlets and methane fractionating column 1 is communicated with.The 2 bottom liquid phases outlets of methane fractionating column backflow separation equipment are gone back and the second inlet of methane fractionating column 1 is communicated with.Be provided with heat exchanger 6 between the charging aperture of the upper end discharging opening of methane fractionating column 1 and methane fractionating column backflow separation equipment 2.
In the present embodiment, heat transmission equipment is plate-fin heat exchanger, and the quantity of plate-fin heat exchanger is not limited to two, can also be provided with three or four, absorption tower 5 can be plate column or packed tower, when absorption tower 5 is plate column, the number of plates is the 3-30 piece, during for packed tower, packed height is 0.1～10 meter, and absorption tower 5 is plate column more preferably.
In the present embodiment, the first liquid phase branch of methane fractionating column backflow separation equipment 2 bottom liquid phases outlets through at least two heat transmission equipment heat-shifts after temperature be the best lower than absorption tower 5 top gas temperature, temperature difference is 0 ℃～200 ℃.If the first liquid phase branch of methane fractionating column backflow separation equipment 2 bottom liquid phases outlets through at least two heat transmission equipment heat-shifts after temperature higher than absorption tower 5 top gas temperature, temperature difference is 0 ℃～50 ℃.
In the present embodiment, the liquid chief component that absorption tower 5 top inlets enter is methane liquid, perhaps hydrogen liquid, perhaps methane and hydrogen mixing material, or methane and hydrogen and ethene mixing material.
the embodiment of the present invention also provides the deep cooling recovery method of ethene in a kind of tail gas, in ethylene production technique through multi-stage condensing, tail gas after separation, still containing the ethene amount is 4% left and right (molar content), all the other main components are methane and hydrogen, contain in addition a small amount of carbon monoxide, after this gas-phase feed is cooled to approximately-97 ℃, the pressure of this moment is about 3.45Mpa, after being cooled to-133 ℃, the first heat transmission equipment 3 enters absorption tower 5, 5 interiorly absorb the cooled gas phase that contains ethene on the absorption tower, isolate the liquid phase part that contains ethene and the gas phase part take methane and hydrogen as main component.Absorption tower 5 interior absorption absorption liquid used be with the Partial Liquid Phase at methane fractionating column 1 top through the first heat transmission equipment 3 and the second heat transmission equipment 4 two-stages cooling after temperature obtain after being down to-151 ℃, absorption liquid enters 5 tops, absorption tower, and the above-mentioned gas phase that contains ethene is absorbed.The gas phase that methane fractionating column 1 is drawn enters methane fractionating column backflow separation equipment 2 after heat exchanger 6 condensations, methane fractionating column backflow separation equipment 2 bottom liquid phases are partly refluxed to methane fractionating column 1, and part is delivered to the first heat transmission equipment 3 and the second heat transmission equipment 4 condensations.
The liquid phase of 5 bottoms, absorption tower enters methane fractionating column 1 as charging after the first heat transmission equipment 3 recovery section colds, the gas phase at 5 tops, absorption tower most of ethene after absorbing is discharged by 5 bottoms, absorption tower with liquid phase, and the gas phase chief component is methane and hydrogen.What 5 tops, absorption tower obtained can further isolate hydrogen take methane and hydrogen as the gas phase of main component after the second heat transmission equipment 4 is cooling, the hydrogen that obtains is through cold recovery, and remaining component obtains the methane hydrogen byproduct take methane as main component after cold recovery.
Adopt this area conventional method to measure the content of ethene in methane hydrogen byproduct, in the present embodiment, the molar content of ethene is about 0.011%.
Fig. 1 is the structural representation of ethene cryogenic recovery system of the prior art, the gas-liquid separation equipment that adopts is rectifying column 51, through multi-stage condensing, it is 4% left and right (molar content) that gas-phase feed after separation contains the ethene amount, all the other main components are methane and hydrogen, contain in addition a small amount of carbon monoxide, the pressure of this moment is about 3.45Mpa, after being cooled to approximately-124 ℃, the 3rd plate-fin heat exchanger 31 enters rectifying column 51, rectifying column 51 bottom liquid phases are sent into ethylene recovery unit after the 3rd plate-fin heat exchanger 31 reclaims cold, rectifying column 51 top gas are isolated liquid phase part and the gas phase part take methane and hydrogen as main component in gas-liquid separation container 6 after the 4th plate-fin heat exchanger 41 cooling segment condensations, liquid phase part refluxes as rectifying column 51, gas phase part further obtains hydrogen after refrigerated separation and the methane hydrogen byproduct take methane as main component is tail gas, the gas that acts as a fuel uses.Adopt conventional method to measure the content of ethene in methane hydrogen byproduct, in this Comparative Examples, the molar content of ethene is 0.13%.
Adopt conventional tower top that the distillation process of condenser is set, the liquid that absorption liquid separates after from the overhead gas partial condensation, this setting is limited by the temperature of the low-temperature receiver that system can provide and the load limit of cold, in the tail gas that tower top obtains, the content of ethene is generally about 0.15%～0.04% (mol), adopt method and system of the present invention, in the tail gas that obtains, ethylene contents is no more than 0.015% (mol), greatly reduce the content of ethene in tail gas, improved ethylene recovery efficient.
The gas phase that the conventional rectification tower obtains is carried out gas-liquid separation again after partial condensation in plate-fin heat exchanger, plate-fin heat exchanger and gas-liquid separation equipment need to be arranged on tower top or higher than a certain position of tower, to guarantee that liquid phase can rely on gravity to realize refluxing, yet this plate-fin heat exchanger and other plate-fin heat exchanger global design and manufacturing, by specialized factory's Design and manufacture, before producer's complete design, with this device-dependent part all can not complete design, it is very large that project duration is affected by it, the shorter project of period ratio particularly, its impact is more obvious.System equipment of the present invention is arranged simple, on the design of device other parts almost without affecting, on project duration without impact.
Adopt conventional absorption tower assimilation effect undesirable, be subject to the composition of ethene absorbing tower top gas and the supply of cold, condensation and separation of liquid measure not enough with respect to the gas phase of tower top, cause in tail gas ethylene contents higher, and due to the absorption liquid quantity not sufficient, capacity of returns is smaller with respect to the gas phase amount, and the design on absorption tower is brought very large inconvenience.The inventive method and system are simple, draw liquid from methane fractionating column backflow separation equipment 2 and are absorbed with following advantage: it is substantially unrestricted 1) to draw flow; 2) simple to operate, flexible; 3) to enter absorption tower 5 front much smaller through the first plate-fin heat exchanger 3 and the second plate-fin heat exchanger 4 cooling procedure institute chilling requirements cold required with respect to the absorption tower 5 tower overhead gas partial condensations of routine, substantially without impact, can not increase system energy consumption to ice chest system cold balancing.
The present invention adopts by drawing one liquid phase as absorption liquid from methane fractionation tower top, this liquid phase cross in plate-fin heat exchanger through at least twice cold after, introduce in the absorption tower ethene in tail gas is absorbed, greatly reduce the content of ethene in tail gas, be that Recovery rate of ethylene improves a lot, and apparatus arrangement is advantages of simple more, overcome the drawback that traditional plate-fin heat exchanger and gas-liquid separation equipment need to be arranged on tower top or bring higher than the position of tower, can not increase equipment size, the reduce cost cost.Absorption liquid is cooling through at least two plate-fin heat exchangers before entering the absorption tower, twice cooling procedure institute chilling requirement is much smaller through the required cold of segregator condensation with respect to the absorption tower top gaseous phase, the present invention substantially without impact, can not increase system energy consumption to ice chest system cold balancing.
The above is only the preferred embodiments of the present invention, is not limited to the present invention, and for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (9)
1. the cryogenic recovery system of ethene in a tail gas is characterized in that: comprise methane fractionating column, methane fractionating column backflow separation equipment, at least two heat transmission equipments and absorption tower, described methane fractionating column top discharge mouth is connected with described methane fractionating column backflow separation equipment charging aperture through heat exchanger, the first liquid phase branch of described methane fractionating column backflow separation equipment bottom liquid phases outlet is connected in series the first heat transmission equipment and the second heat transmission equipment successively, the bottom import of described absorption tower is communicated with described the first heat transmission equipment outlet, the gas phase import of described absorption tower top gaseous phase outlet and described the second heat transmission equipment is communicated with, top, described absorption tower inlet is communicated with the liquid-phase outlet of described the second heat transmission equipment, bottom, described absorption tower liquid-phase outlet is communicated with described the first heat transmission equipment bottom import, described the first heat transmission equipment bottom liquid-phase outlet is communicated with the first inlet of described methane fractionating column.
2. the cryogenic recovery system of ethene in tail gas as claimed in claim 1, it is characterized in that: described absorption tower is plate column, the number of plates of described plate column is the 3-30 piece.
3. the cryogenic recovery system of ethene in tail gas as claimed in claim 1, it is characterized in that: described absorption tower is packed tower, the packed height of described packed tower is 0.1～10 meter.
4. the cryogenic recovery system of ethene in tail gas as claimed in claim 1, it is characterized in that: after the first described at least two heat transmission equipment heat-shifts of liquid phase branch's process of described methane fractionating column backflow separation equipment bottom liquid phases outlet, temperature is lower than described absorption tower top gas temperature, and temperature difference is 0 ℃～200 ℃.
5. the cryogenic recovery system of ethene in tail gas as claimed in claim 1, it is characterized in that: after the first described at least two heat transmission equipment heat-shifts of liquid phase branch's process of described methane fractionating column backflow separation equipment bottom liquid phases outlet, temperature is higher than described absorption tower top gas temperature, and temperature difference is 0 ℃～50 ℃.
6. the cryogenic recovery system of ethene in tail gas as claimed in claim 1, it is characterized in that: described at least two heat transmission equipments are plate-fin heat exchanger.
7. the cryogenic recovery system of ethene in tail gas as claimed in claim 1, it is characterized in that: the liquid that top, described absorption tower inlet enters is methane liquid, perhaps hydrogen liquid, perhaps methane and hydrogen mixing material, or methane and hydrogen and ethene mixing material.
8. the cryogenic recovery system of ethene in tail gas as claimed in claim 1 is characterized in that: described methane fractionating column backflow separation equipment bottom liquid phases outlet is communicated with the second inlet of described methane fractionating column.
9. the deep cooling recovery method of ethene in a tail gas, is characterized in that, comprises the steps:
The tail gas that (1) will contain ethene absorbs the described cooled tail gas that contains ethene in the absorption tower after the first heat transmission equipment is cooling, isolates the liquid phase part that contains ethene and the gas phase part take methane, hydrogen as main component;
(2) liquid phase part that contains ethene after described separation reclaims cold through the first heat transmission equipment, and the liquid phase after cold recovery is returned to the methane fractionating column, sends into ethylene column after the lower end discharging opening outflow of described methane fractionating column, isolates ethylene product; Simultaneously, after described separation take methane, hydrogen as main gas phase part after the second heat transmission equipment refrigerated separation, isolate hydrogen product and methane hydrogen byproduct;
In described step (1), absorbing absorption liquid used in described absorption tower and be the Partial Liquid Phase that described methane fractionating column top is obtained, to introduce described absorption tower after at least two heat transmission equipments are cooling resulting.
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| CN201110385660.2A CN103127802B (en) | 2011-11-28 | 2011-11-28 | Cryogenic recovery system and recovery method for ethylene in tail gas |
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| CN201110385660.2A CN103127802B (en) | 2011-11-28 | 2011-11-28 | Cryogenic recovery system and recovery method for ethylene in tail gas |
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| CN103127802B CN103127802B (en) | 2014-11-26 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106268235A (en) * | 2016-09-28 | 2017-01-04 | 中石化节能环保工程科技有限公司 | Oil field fuel oil injection boiler tail gas desulfurization denitration processing system |
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|---|---|---|---|---|
| CN1048713C (en) * | 1996-10-29 | 2000-01-26 | 倪进方 | Light hydrocarbon separation method capable of raising ethylene recovery |
| CN1715260A (en) * | 2004-07-02 | 2006-01-04 | 凯洛格.布朗及鲁特有限公司 | Low pressure olefin recovery process |
| US7763165B1 (en) * | 2006-12-21 | 2010-07-27 | Uop Llc | Fractionation recovery processing of FCC-produced light olefins |
| CN101967077A (en) * | 2009-07-27 | 2011-02-09 | 中国石油天然气股份有限公司 | Ethylene device front-end deethanization separation process |
| CN202315648U (en) * | 2011-11-28 | 2012-07-11 | 中国石油天然气集团公司 | Cryogenic recovery system for ethylene in tail gas |
-
2011
- 2011-11-28 CN CN201110385660.2A patent/CN103127802B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1048713C (en) * | 1996-10-29 | 2000-01-26 | 倪进方 | Light hydrocarbon separation method capable of raising ethylene recovery |
| CN1715260A (en) * | 2004-07-02 | 2006-01-04 | 凯洛格.布朗及鲁特有限公司 | Low pressure olefin recovery process |
| US7763165B1 (en) * | 2006-12-21 | 2010-07-27 | Uop Llc | Fractionation recovery processing of FCC-produced light olefins |
| CN101967077A (en) * | 2009-07-27 | 2011-02-09 | 中国石油天然气股份有限公司 | Ethylene device front-end deethanization separation process |
| CN202315648U (en) * | 2011-11-28 | 2012-07-11 | 中国石油天然气集团公司 | Cryogenic recovery system for ethylene in tail gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106268235A (en) * | 2016-09-28 | 2017-01-04 | 中石化节能环保工程科技有限公司 | Oil field fuel oil injection boiler tail gas desulfurization denitration processing system |
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