CN1762929A - Hydration, pressure swing adsorption and deep cooling combined process for separating ethene cracking gas - Google Patents
Hydration, pressure swing adsorption and deep cooling combined process for separating ethene cracking gas Download PDFInfo
- Publication number
- CN1762929A CN1762929A CN 200510105304 CN200510105304A CN1762929A CN 1762929 A CN1762929 A CN 1762929A CN 200510105304 CN200510105304 CN 200510105304 CN 200510105304 A CN200510105304 A CN 200510105304A CN 1762929 A CN1762929 A CN 1762929A
- Authority
- CN
- China
- Prior art keywords
- methane
- gas
- separation
- hydrate
- hydration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention proposes one method of separating ethylene cracking gas, is one combined separation process including hydrating separation, cryogenic separation and PSA separation, and aims at applying new hydrating separation process in the separation of ethylene cracking gas. First, reaction condition is controlled for the C2 component in the cracked gas to form hydrate prior and to be separated. Then, the cold produced by the expanding methane and hydrogen flow is used as the cold source for the methane eliminating tower, and PSA separation is combined to realize the separation of hydrogen, methane and C2 component ultimately. The present invention has no stage-by-stage condensation steps and cold casing and thus lowered cold load of the methane eliminating tower.
Description
Technical field
The present invention relates to the separating technology of ethene cracking gas, relate in particular to the combination process flow process that hydration separation technology, subzero fractionation and transformation adsorptive separation technology is combined separating ethene cracking gas, belong to the chemical industry technology.
Background technology
Ethylene industry always occupies critical role as the mainstay industry of petrochemical industry in national economy.Along with the development and the requirement of each side, there is expansion energy synergic pressure mostly in existing ethylene unit.The most complicated part is exactly a deep cooling demethanizing workshop section in cracking of ethylene and the separating technology, and the deep cooling demethanizing device that generally adopts is that whole device expands energy synergic bottleneck especially at present.
In the separation process of deep cooling demethanizing, two key links are arranged, first demethanizing tower, it two is ice chests.Because the demethanizing tower temperature requirement is minimum, it is the place that consumes the cold maximum, the technological operation complexity, for the separation between the various micro-molecular gas, adopt the conventional rectification method under very low temperature, to realize, as need separating of methane and hydrogen carry out about-160 ℃, methane and need about-110 ℃, carry out separating of ethane, cause the pre-cold-peace demethanizing tower of raw material system cold in whole sepn process to consume shared proportion maximum.Have data to propose, the cold of demethanizing tower system accounts for 42% of sepn process total amount consumption.Ice chest is owing to service temperature very low (160 ℃), and very harsh to the requirement of material, manufacturing cost is very high, and may set off an explosion because of generating Lan Binger.Therefore ice chest and demethanizing tower become the bottleneck of existing installation capacity expansion revamping, also are the new very high reasons of production ethylene unit construction investment simultaneously.So seek a kind of technology more energy-conservation, separating hydrogen gas, methane and C2 component (ethene and ethane) efficiently for the energy consumption that reduces separating ethene cracking gas technology in the ethylene industry, increase economic efficiency, have important practical significance.
Hydrate is water and micro-molecular gas (CH
4, C
2H
6, CO
2, N
2Deng) a kind of cage modle material (water molecules constitutes the cage that is connected with each other aloft by hydrogen bond, and gas molecule is in the cage to keep the stability of cage) of under certain temperature, pressure condition, forming.The complexity that forms hydrate owing to gas with various is different, therefore can make the gaseous fraction of easy generation hydrate preferentially enter the hydrate phase and realize separation of gaseous mixture by generating the method for hydrate.As known general knowledge, generally speaking, have only micro-molecular gas could generate hydrate, therefore hydrate only is fit to separate the low-boiling point gas mixture usually, and the sharpest edges of hydrate are can be in the separation that realizes the low-boiling point gas mixture more than 0 ℃, and boiling point not to be very low mixture separate more effective with the rectificating method of routine.
Hydrate Technology is in present research and use present situation more aspect the storage and transportation of gas, how other operations such as Hydrate Technology and for example gas delivery is combined, and does not also more report.
Summary of the invention
The present invention proposes a kind of separating ethene cracking gas technology that is different from conventional art, hydration separation, transformation fractionation by adsorption are combined with the low temperature separation process of methane, when obtaining high-purity C 2 components, can save workshop section of condensation step by step and ice chest in the traditional technology, and reduction demethanizer column overhead refrigeration duty, thereby reduce the production energy consumption and the cost input of ethylene industry, improve productivity effect.
The present invention mainly provides a kind of combination process that is used for separating ethene cracking gas, and the combination that it has comprised hydration separation, low temperature separation process and transformation adsorption separation technology can realize that hydrogen in the splitting gas, methane separate with the C2 component, and this combination process process comprises:
Splitting gas to be separated at first enters the hydration separation unit, and contacts with liquid, aqueous, and the control hydrating condition makes the C2 component in the splitting gas preferentially form hydrate, and splitting gas is separated into the methane+C2 logistics of methane+hydrogen gaseous stream and hydrate forms;
Methane+C2 logistics enters the deep cooling demethanizing tower after dissolving, dewater, cooling off, realize the fine separation of methane and C2 component, and methane stream is carried out swell refrigeration, for demethanizing tower provides cold;
The gaseous stream that obtains in the hydration separation process enters and separates in the transformation fractionation by adsorption device after providing cold through dehydration, precooling, expansion and for demethanizing tower, obtains purified hydrogen and methane gas.
In the method for separating ethene cracking gas provided by the invention, what splitting gas to be separated at first entered is the hydration separation unit, in this unit, be separated into methane+hydrogen (gas phase) and two bursts of logistics of methane+C2 (hydrate slurry), this moment, most C2 components became hydrate with the small portion methane conversion, that is, the task of the C2 component in the separating and cracking gas has significantly been born in hydration separation of the present invention unit.The unitary operation of described hydration separation comprises makes splitting gas to be separated and liquid, aqueous reverse the contact, wherein C2 component and part methane generate hydrate in hydration reactor, and make that the slurries of this hydrate and gas phase separation are laggard goes into hydrate and dissolve device and be decomposed and discharge the process of C2 component and methane.Concrete, can make splitting gas to be separated enter the hydration reaction tower from the bottom, in up process with descending liquid, aqueous Continuous Contact, in this process, can realize C2 component more than 99% and small portion methane generation hydrate (slurries) in the splitting gas, hydrate slurry comes out from hydration reaction tower bottom, enter hydrate and dissolve device, the methane that discharges after dissolving+C2 component mixed gas logistics is left the hydration separating unit and enter the deep cooling demethanizing tower again after dehydration, cooling.Leave main hydrogen and methane in the gas phase of hydration reaction tower, the volumetric molar concentration of C2 component wherein is less than 1%, through dehydration, precooling, expansion can be demethanizing tower that cold is provided, then this gas stream enters in the transformation fractionation by adsorption device and separates, and obtains purified hydrogen and methane gas.
The method of the present invention and the traditional separating ethene cracking gas technology key distinction are at first to adopt the hydration technology to make the C2 component form hydrate earlier, separate with most of methane gas with hydrogen, this moment has a small amount of methane and the C2 component forms hydrate simultaneously, so, methane content is very low in the gas phase after the decomposition of hydrate, and needed cold load is very little when demethanizing technology is separated again.Hydrate dissolve dissolve in the device obtain liquid, aqueous can through the cooling after return hydrate reactor, recycle.
The combined technical method of separating ethene cracking gas provided by the invention, be to utilize self system to separate the methane and the methane+hydrogen gas stream that obtain to carry out swell refrigeration, for demethanizing tower provides cold, whole process can not need extra cryogenic refrigeration, that is, do not need workshop section of condensation step by step and ice chest in the traditional technology fully.Owing to methane in the gas mixture that enters demethanizing tower reduces in a large number, can significantly reduce the logistics load and the refrigeration duty of demethanizing tower simultaneously, thereby reduce the whole energy consumption of separating ethene cracking gas technology, increase economic efficiency, should have important practical significance.
It needs to be noted that the design philosophy of the technology of the present invention is to allow C2 component in the splitting gas have precedence over methane generate hydrate, to improve the initial gross separation efficient of methane and C2 component in the hydration reaction tower.From the split product that pyrolyzer comes, contain more C3 (propane, propylene) and above component usually, their existence has side effect to the separating effect of methane and C2 component, therefore the logistics that adopts the inventive method to require to enter the hydration reaction tower should be from split product, separated after most of C3 and the above heavy constituent the lightweight logistics (promptly, main hydrogen, methane, ethane, ethene etc.), C3 wherein and above heavy constituent content preferably are controlled at and are lower than 2% volumetric molar concentration.Simultaneously, in the hydration reaction system, should not contain and help the material that methane generates hydrate, as propane, propylene, butane, pentamethylene, tetrahydrofuran (THF) etc.This case applicant has formerly patent put down in writing this content, patent No. ZL02129611.1, wherein materials such as pentamethylene, tetrahydrofuran (THF) are promoted methane to generate hydrate as having necessarily optionally thermodynamics promotor use, reaching, suppress the purpose that C2 generates hydrate.
Among the present invention, separating effect and raising hydrate formation speed for methane and C2 in the raising hydro-combination process, except that avoiding above-mentioned unfavorable factor, also can take one of following measure to increase hydro-combination process to the C2 components selection: (1) liquid, aqueous employing contains and can have the aqueous solution of the additive of solublization to C2 component (especially to ethene), for this additive multiple choices can be arranged, it can be anion surfactant, especially can be the high fatty alcohol sulfuric acid ester in the anionic surface active substances, as sodium lauryl sulphate (having another name called " sodium laurylsulfate "), Sodium palmityl sulfate (having another name called " hexadecanol sodium sulfate "), sodium stearyl sulfate (having another name called " stearyl alcohol sodium sulfate ") etc.; It also can be the polymkeric substance of the water-soluble or water dispersible class of vinyl lactam monomer, polymkeric substance, mixture; Or some ionic compounds, for example NaF, MgF
2, SrF
2, BaF
2, NaCl, CaCl
2, MgCl
2, CaSO
4, Na (ClO
4), NaH
2PO
4, Na
2HPO
4Deng; According to the specific nature of additive, its concentration in liquid, aqueous preferably is controlled at 300～1000mg/ liter; (2) emulsion (emulsion) that forms by water and hydrocarbon liquids of liquid, aqueous employing, described hydrocarbon liquids is C6 or above pure alkane or the hydrocarbon mixture (as gasoline, kerosene, diesel oil etc.) of C6, energy optimum solvation C2 component behind this hydrocarbon liquids and the water formation emulsion, multimachine can preferentially contact with water and generate hydrate to make it have more, and the profit volume ratio is 1: 1～4: 1.Preparation can be adopted suitable emulsifying agent during emulsion, for example sapn series etc.
In the technical process of the present invention, the concrete formation condition of hydrate and dissolve condition be those skilled in the art can grasp, a lot of researchs have been arranged.Generally speaking, should control the interior temperature of hydration reaction tower between-15～10 ℃, pressure-controlling is between 1～8MPa, generate hydrate (have a small amount of methane and generate hydrate simultaneously) to help the C2 component, according to the character of gas mixture and the needs of separation accuracy, when the service temperature in the hydration reaction tower below 0 ℃ the time, the emulsion that the liquid, aqueous preferred employing in the hydration reaction system is formed by water and hydrocarbon liquids.The temperature that hydrate is dissolved in the device should be controlled between 15～50 ℃, and the operational requirement that pressure should satisfy the deep cooling demethanizing tower gets final product (generally speaking greater than 3.0MPa).
By above-mentioned hydration separation unit, though can realize that splitting gas separates significantly, the purity of the ethene that obtains after separating still can not reach requirement, wherein also is entrained with the methane of small portion, needs further to separate to purify.Concrete steps comprise: dissolve the methane+C2 mixed gas logistics that discharges after device is dissolved from the unitary hydrate of hydration separation, after dehydration, cooling, enter the deep cooling demethanizing tower, in demethanizing tower, realize the fine separation of methane and C2 component, operational condition in this demethanizing tower is identical with traditional technology, is known in those skilled in the art.Among the present invention, carry out swell refrigeration, directly provide the part cold for demethanizing tower in demethanizing tower, separating the methane gas logistics that obtains.
On the other hand, the gaseous stream that comes out from the hydration reaction tower comprises is significantly put forward dense hydrogen and the most of methane gas the unstripped gas, according to technology of the present invention, dehydration, precooling, expansion are implemented in this logistics, for demethanizing tower provides the part cold in addition, and then, obtain purified hydrogen and methane gas to this gas stream enforcement transformation fractionation by adsorption.
The front is mentioned, it is known technology that the gas that relates among the present invention forms Hydrate Technology itself, and the transformation adsorption separation technology of used gas expansion refrigeration and mixed gas and install also all and to be known technology in the industry, so the concrete operations the present invention who relates to these technology does not do detailed description.
In sum, the combined technical method that hydration separation, low temperature separation process and transformation fractionation by adsorption are combined of the present invention can be applicable to transform existing ethene cracking gas separation process, comprises order separation process and predepropanization (C3 component) separation process.Point of penetration is selected in the logistics incision of having taken off most of C3 and above component from split product, mainly utilize the initial gross separation of hydration separation technology realization to hydrogen, methane and C2 in the ethene cracking gas, the methane that enters demethanizing tower is reduced in a large number, significantly reduce the logistics load and the refrigeration duty of demethanizing tower; And utilize the methane stream that obtains in the sepn process to provide demethanizing tower needed cold by precooling, the back of expanding, thus can remove tradition condensation workshop section and ice chest step by step, increase economic efficiency.For improving the effect of hydration separation, preferably give suitable compression earlier for the splitting gas of cutting flow process of the present invention, splitting gas pressure is adjusted to about 3.6～5.0MPa.
Owing to adopted the method for traditional rectifying to realize the fine separation of methane and C2 (ethane and mixture of ethylene), can obtain high-purity product simultaneously.In other words, combination process of the present invention had both been avoided complicated refrigeration and heat exchange operation, had saved energy expenditure, and product is met the demands, and had superior advance and practicality.
Description of drawings
Fig. 1 is a combination process schematic flow sheet of the present invention.
Embodiment
Below in conjunction with accompanying drawing and specific embodiments the present invention is introduced in more detail, but but practical range of the present invention is not constituted any qualification.
Please shown in Figure 1 in conjunction with consulting, the method for separating ethene cracking gas of the present invention is to adopt the combination process that comprises hydration separation, low temperature separation process and the operation of transformation fractionation by adsorption, and its main technique flow process is:
The logistics of the light component (hydrogen, methane, C2 (mixture of ethane+ethene) etc.) of split product after having separated the above heavy constituent of C3 enters the hydration reaction tower from the bottom, generate gas hydrate with descending liquid, aqueous Continuous Contact in up process; As long as the hydrating condition of control methane, C2 component in the gas mixture (ethane, ethene) will preferentially generate hydrate, become hydrate slurry together with a small amount of methane hydrate and emit from the reaction tower bottom and enter hydrate and dissolve device, hydrogen, methane are carried dense in gas phase.
The hydrate slurry that obtains from the hydration separation process enters hydrate to be dissolved device and is become ethane, the ethene mixed air that contains a small amount of methane after dissolving, and enters the deep cooling demethanizing tower after the dehydration, realizes the fine separation of methane and C2 component.Highly purified C2 (gas mixture of ethene and ethane) is collected as final product, methane stream after the fine separation by pre-cold-peace swell refrigeration, provides cold through heat exchanging process for follow-up deep cooling demethanizing by swell refrigeration mechanism (the interior part of frame of broken lines among the figure).Hydrate dissolve dissolve in the device obtain liquid, aqueous through the cooling after also can return hydrate reactor, be recycled.
Carried dense gaseous stream in the hydration separation process and after dehydration, also be inflated refrigeration by swell refrigeration mechanism, for follow-up deep cooling demethanizing provides cold, and this gaseous stream enters subsequently and separates in the transformation fractionation by adsorption device, obtains purified hydrogen and methane gas respectively.As seen, whole technological process can not need extra cryogenic refrigeration equipment and operation.
Deep cooling demethanizing wherein, transformation fractionation by adsorption hydrogen and methane, and the precooling expansion process of gas all is the routine techniques of gas delivery and ethene cracking gas demethanizing with device, and described hydration reaction tower (or reactor) is meant the reaction unit that can make unstripped gas and aqueous fluid physical efficiency fully contact the generation hydrate therein, not particular requirement, it for example can be withstand voltage reactor, in actual production, can adopt tower hydration reactor to realize stage trapping, described tower hydration reactor is not special design, its internal structure can be similar with the multistage rectification tower structure, the abundant contact that more helps gas-liquid with separate.
The separating effect and the energy consumption analysis of embodiment 1, hydration separation+transformation fractionation by adsorption+deep cooling separation combined process flow processing ethene cracking gas
Present embodiment separates the analog vinyl splitting gas according to the combination process flow process of the invention described above, writes down its separating effect data, and the heat energy consumption in its process is analyzed.
(mol%) formed in analog vinyl splitting gas (unstripped gas) logistics:
H
2，19.85％；CH
4，42.78％；C
2H
4，33.78％；C
2H
6，2.41％；C
3H
6，0.35％。
Concrete technical process:
Hydration reactor is at first sent in splitting gas logistics to be separated (the about 3.6MPa of pressure of splitting gas at this moment), is the hydration reaction tower that can realize stage trapping among this embodiment.Hydration reaction tower operational condition: 1 ℃ of temperature, pressure 5MPa, the emulsion of liquid, aqueous employing water+diesel oil, the profit volume ratio is about 2: 1, about 75: 1 of gas-liquid volume ratio.
Form two bursts of logistics after above-mentioned hydration separation: the gaseous stream after stage trapping is hydrogen+methane blended gas (H
2(60.06%)+CH
4(39.94%)), isolated liquid phase soup compound is decomposed into gas phase (dissolving in the device through heating up and suitably step-down) again through dissolving device, consists of methane, ethane, ethene and propylene gas mixture (CH
4(10.01%)+C
2H
4(78.56%)+C
2H
6(9.34%)+C
3H
6(2.09%)).Liquid, aqueously send the hydration reactor recycle back to.
Enter the deep cooling demethanizing tower from dissolving the gas mixture that device comes out, realize separating of methane and C2 and above component, test result shows that the yield of ethene can reach 99.8%, and methane gas provides low-temperature receiver through swell refrigeration to demethanizing tower.
The gaseous stream of telling from the hydration reaction tower (gas mixture of hydrogen and methane) dewaters earlier, carrying out precooling then expands, for demethanizing tower provides the cold source, mixed gas after the heat exchange enters transformation adsorptive reactor (the PSA technology that adopts industry to know under the condition of 50 ℃ and 5MPa, utilize the multitower pressure swing adsorption technique to implement, working pressure is 1.0MPa), obtain being put forward dense hydrogen and methane gas, wherein the concentration of hydrogen can be carried dense to more than 96%.
Through above process, can obtain hydrogen, C2 gas (ethene, ethane and a small amount of propylene) and methane gas respectively.
Below be to the traditional predepropanization deep cooling process for separating flow process and the energy consumption analysis and the comparison of combination process of the present invention:
Analyze benchmark---feed gas stream is formed (H
2, 19.85%; CH
4, 42.78%; C
2H
4, 33.78%; C
2H
6, 2.41%; C
3H
6, 0.35%), raw gas flow 1290Kmol/h;
Described traditional predepropanization deep cooling process for separating is meant the common process that present ethylene gas is produced, and only its energy consumption is calculated at this, and technology is not described in more detail.
1. adopt traditional predepropanization deep cooling process for separating flow process:
The outer total heat duties (2.08mmkcal/h) of energy expenditure total amount=ice chest thermal load (2mmkcal/h)+ice chest+demethanizing cat head condensation load (1.64mmkcal/h)+demethanizer bottoms load (1.6mmkcal/h)=7.32mmkcal/h that boils again;
2. adopt the combination process flow process of the embodiment of the invention 1:
The thermal load of energy expenditure total amount=hydration reactor (2.10mmkcal/h)+splitting gas is compressed to the isolating energy material of power (0.30mmkcal/h)+absorption transformation consumption (0.95mmkcal/h)+demethanizing cat head condensation load (0.48mmkcal/h)=3.83mmkcal/h that 5MPa needs from 3.6MPa;
Annotate: comprised the energy consumption of compressing, cracking gas in the above calculating, but this step is in order to improve separation efficiency, optional, if the unstripped gas that inserts is directly carried out hydration separation, then total energy consumption also will be lower than above measuring and calculating.
So when adopting combination process separating ethene cracking gas of the present invention, energy can save at least 45%.
By preliminary Technological Economy analysis in the present embodiment as can be known, after having adopted combination process flow process of the present invention that ethene cracking gas is separated, flow rate of methane descends more than 70% in the demethanizing tower, hydration cat head C2 content is less than 0.8～1.0%, methane and hydrogen are used to demethanizing tower that the part cold is provided earlier, utilize the transformation fractionation by adsorption again.Compare with traditional low temperature separation process, adopt combination process flow process separating ethene cracking gas of the present invention can save the energy consumption of low temperature separation process more than 40%; In addition, the simple hydration separation method that adopts, though can realize that splitting gas separates significantly, but the purity of ethene can not reach requirement, and employing the present invention, allow hydration separation bear most of separation task, realize the fine separation of methane and C2 (ethane and ethene) obtaining high-purity product with the method for traditional rectifying.Complicated refrigeration and heat exchange operation both avoided in such combination, saved energy expenditure, and product is met the demands, and the ethylene recovery rate can reach 99.8%, and purity also can meet the demands.Owing to the methane that enters demethanizing tower reduces in a large number, can significantly reduce the logistics load and the refrigeration duty of demethanizing tower simultaneously, therefore have revolutionary meaning.
Embodiment 2, contain the single-stage hydration separation of the water liquid separation ethene cracking gas of SDS (500ppm)
Hydration reaction condition: T=275.15K, P=3MPa, the air water volume ratio is 75: 1.
Experimental technique: splitting gas mixed gas to be separated contacts in autoclave with liquid, aqueous, the water generation reaction compound.Keep temperature of reaction and constant pressure in the reaction process, after reaction reaches balance, analyze the gas composition that discharges after gas phase composition and hydrate are dissolved respectively.
The gas composition that discharges after hydrate is dissolved is exactly the butt composition (having deducted the later gas composition of the water yield) of hydrate phase.
Table 1, contain the single-stage hydration separation effect of the water liquid separation ethene cracking gas of SDS (500ppm)
| The component title | Unstripped gas is formed (mol%) | Gas phase is formed (mol%) | The hydrate phase composite (butt, mol%) |
| H2 | 18.27 | 60.25 | 10.65 |
| CH4 | 30.33 | 25.16 | 30.42 |
| C2H4 | 35.88 | 10.36 | 41.14 |
| C2H6 | 5.0 | 1.68 | 5.12 |
| C3H6 | 10.48 | 2.55 | 12.67 |
The single-stage hydration separation of separating ethene cracking gas during the emulsion of embodiment 3, liquid, aqueous employing water+diesel oil
Hydration reaction condition: T=274.15K, P=5MPa, the profit volume ratio is 2: 1, adopts emulsifier span 20 to make the water-in-oil emulsion system, the gas-liquid volume ratio that enters the hydration reaction tower is 75: 1;
Experimental technique is identical with embodiment 2.
The single-stage hydration separation effect of separating ethene cracking gas during the emulsion of table 2, liquid, aqueous employing water+diesel oil
| The component title | Unstripped gas is formed (mol%) | Gas phase is formed (mol%) | The hydrate phase composite (butt, mol%) |
| H2 | 18.27 | 65.35 | 9.78 |
| CH4 | 30.33 | 24.18 | 31.44 |
| C2H4 | 35.88 | 8.37 | 40.84 |
| C2H6 | 5.0 | 1.08 | 5.71 |
| C3H6 | 10.48 | 1.02 | 12.21 |
Embodiment 4, contain the single-stage hydration separation of the water liquid separation ethene cracking gas of poly N-vinyl lactan (650ppm)
Hydration reaction condition: T=275.15K, P=3MPa, the air water volume ratio is 75: 1;
Experimental technique is identical with embodiment 2.
Table 3, contain the single-stage hydration separation effect of the water liquid separation ethene cracking gas of poly N-vinyl lactan (650ppm)
| The component title | Unstripped gas is formed (mol%) | Gas phase is formed (mol%) | The hydrate phase composite (butt, mol%) |
| H2 | 19.85 | 44.58 | 0.98 |
| CH4 | 42.78 | 48.31 | 38.86 |
| C2H4 | 33.78 | 6.52 | 54.64 |
| C2H6 | 2.41 | 0.26 | 3.72 |
| C3H6 | 1.18 | 0.33 | 1.80 |
From the listed result of table 2 as can be seen, during the emulsion of liquid, aqueous employing water+diesel oil, C2 is that major part is transferred to the hydrate phase after the flash liberation, and that methane obtains carrying in gas phase is dense, and hydrogen has then almost all been stayed gas phase, shows that the hydration separation effect is good.In addition, classify single equilibrium stage separating effect in the table 2 as.The hydration separation process that takes place in the tower hydration reactor that adopts among the present invention is a multi-stage separation process, and effect can be separated much better than single-stage.
From table 2 and the listed result of table 3 to recently, when C3 content more for a long time, the separating effect of methane and C2 obviously reduces.The emulsion that liquid, aqueous employing water and other hydrocarbon liquids (as normal heptane, octane, kerosene etc.) are formed can obtain similar result.
Claims (10)
1, a kind of combination process that is used for separating ethene cracking gas, the combination that it has comprised hydration separation, low temperature separation process and the operation of transformation fractionation by adsorption can realize that hydrogen in the splitting gas, methane separate with the C2 component, this combination process process comprises:
Splitting gas to be separated at first enters the hydration separation unit, and contacts with liquid, aqueous, and the control hydrating condition makes the C2 component in the splitting gas preferentially form hydrate, and splitting gas is separated into the methane+C2 logistics of methane+hydrogen gaseous stream and hydrate forms;
Methane+C2 logistics enters the deep cooling demethanizing tower after dissolving, dewater, cooling off, realize the fine separation of methane and C2 component, and the methane stream of telling is carried out swell refrigeration, for demethanizing tower provides cold;
The gaseous stream that obtains in the hydration separation process enters in the transformation fractionation by adsorption device after providing cold through dehydration, precooling, expansion and for demethanizing tower, obtains purified hydrogen and methane gas through lock out operation.
2, the described combination process of claim 1, the unitary operation of described hydration separation comprises makes splitting gas to be separated and liquid, aqueous reverse the contact, wherein C2 component and part methane generate hydrate in hydration reactor, and make that the slurries of this hydrate and gas phase separation are laggard goes into hydrate and dissolve device and be decomposed and discharge the process of C2 component and methane.
3, claim 1 or 2 described combination procesies, wherein, described splitting gas to be separated is the lightweight stream feed gas that has separated after most of C3 and the above heavy constituent, C3 wherein and above component concentration are lower than 2% volumetric molar concentration.
4, the described combination process of claim 2, wherein, described hydrate is dissolved liquid, aqueous that decomposition obtains in the device and return hydrate reactor after cooling, recycles.
5, each described combination process of claim 1～4, wherein, take one of following measure to increase hydro-combination process to the C2 components selection: (1) is adopted and is contained additive liquid, aqueous that the C2 component is had solublization, and the concentration of additive is controlled at 300～1000mg/ liter; (2) emulsion that formed by water and hydrocarbon liquids of liquid, aqueous employing, described hydrocarbon liquids are C6 or above pure alkane or the hydrocarbon mixture of C6.
6, the described combination process of claim 5, wherein, the described additive that C2 is had a solublization is selected from anionic surface active substances, the polymkeric substance of the water-soluble or water dispersible of vinyl lactam monomer, polymkeric substance, mixture, or ionic compound; Described hydrocarbon mixture with water formation emulsion is gasoline, kerosene or diesel oil, and the profit volume ratio is 1: 1～4: 1.
7, each described combination process of claim 1～4, wherein, operating in the hydration reactor of described formation hydrate finished, and service temperature is between-15～10 ℃, and pressure is between 1～8MPa.
8, the described combination process of claim 5, wherein, operating in the hydration reactor of described formation hydrate finished, and service temperature is between-15～10 ℃, and pressure is between 1～8MPa.
9, each described combination process of claim 1～4, wherein, described hydrate is dissolved the interior service temperature of device between 15～50 ℃, and pressure is greater than 3.0MPa.
10, each described combination process of claim 1～4, wherein, described splitting gas to be separated is before entering the hydration separation unit, and pressure is 3.6～5.0MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101053045A CN100404483C (en) | 2005-09-23 | 2005-09-23 | Hydration, pressure swing adsorption and deep cooling combined process for separating ethene cracking gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101053045A CN100404483C (en) | 2005-09-23 | 2005-09-23 | Hydration, pressure swing adsorption and deep cooling combined process for separating ethene cracking gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1762929A true CN1762929A (en) | 2006-04-26 |
| CN100404483C CN100404483C (en) | 2008-07-23 |
Family
ID=36747288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005101053045A Expired - Fee Related CN100404483C (en) | 2005-09-23 | 2005-09-23 | Hydration, pressure swing adsorption and deep cooling combined process for separating ethene cracking gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100404483C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109420419A (en) * | 2017-08-20 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of decomposition of hydrate device, mixed gas separation system and separation method |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1188375C (en) * | 2001-05-25 | 2005-02-09 | 清华大学 | Method for demethanizing in ethylene production |
| CN1258391C (en) * | 2003-04-14 | 2006-06-07 | 中国石油化工股份有限公司 | Method for separating low boiling point gas mixture using hydrate method and its system |
-
2005
- 2005-09-23 CN CNB2005101053045A patent/CN100404483C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109420419A (en) * | 2017-08-20 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of decomposition of hydrate device, mixed gas separation system and separation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100404483C (en) | 2008-07-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1847203A (en) | Separating method for converting methanol to prepare low carbon olefin gas | |
| Benali et al. | Ethane/ethylene and propane/propylene separation in hybrid membrane distillation systems: Optimization and economic analysis | |
| CN101063048A (en) | Method for separating plant catalytic dry gas by employing middle-cool-oil absorption process | |
| CN1096440C (en) | Improved chemical absorption process for recovering olefins from cracked gases | |
| CN1305551C (en) | Process of absorption-hydration coupling for separating multicomponent gas mixture | |
| CN1258391C (en) | Method for separating low boiling point gas mixture using hydrate method and its system | |
| CN106316752A (en) | Separation method for methanol-to-propylene (MTP) reaction product | |
| CN103242123B (en) | A kind of separation method of low carbon olefin gas | |
| CN101978028A (en) | Separation process for olefin production | |
| CN101973831A (en) | Separation method for producing light olefins from oxygenated chemicals | |
| WO2020073853A1 (en) | Method and system for separating light hydrocarbons | |
| CN103159581B (en) | A kind of system and method for absorption extraction catalytic pyrolysis gas product polymerization-grade propylene | |
| CN108610229B (en) | Light hydrocarbon separation system and method | |
| CN100475933C (en) | Combined process for separating and recovering hydrogen, ethylene and ethane from refinery dry gas or separating ethylene cracking gas | |
| CN102304010A (en) | Method for separating low carbon olefin mixed gas by rectifying and absorbing | |
| CN1762930A (en) | Secondary hydration and deep cooling separation combined process for separating ethene cracking gas | |
| CN103772106B (en) | For reclaiming ethene in catalytic cracked dry gas or ethene cracking gas, the hydration of ethane absorbs the device and method of air lift | |
| CN1157280A (en) | Light hydrocarbon separation method capable of raising ethylene recovery | |
| CN1407304A (en) | Improved light hydrocarbon deep cooling separating method | |
| CN1919975A (en) | Technique of separating and recovering lighter hydrocarbons in refinery dried gas | |
| CN103030494B (en) | Absorption and hydration coupling device and method for separating ethylene and ethane in catalytic cracking dry gas or ethylene pyrolysis gas | |
| CN112358375B (en) | Two-tower double-heat-pump integrated 1-butene refining energy-saving process and device | |
| CN109701364B (en) | System and method for separating gas by hydration method | |
| CN1762928A (en) | Hydration, film and deep cooling separation combined process for separating ethene cracking gas | |
| CN109678636A (en) | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080723 Termination date: 20120923 |