CN1106055A - Catalytic cracking process - Google Patents
Catalytic cracking process Download PDFInfo
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- CN1106055A CN1106055A CN 94118602 CN94118602A CN1106055A CN 1106055 A CN1106055 A CN 1106055A CN 94118602 CN94118602 CN 94118602 CN 94118602 A CN94118602 A CN 94118602A CN 1106055 A CN1106055 A CN 1106055A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/046—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by adsorption, i.e. with the use of solids
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
A hydrocarbon stream is cracked to produce a hot gaseous stream which is compressed and cooled to condense almost all of the hydrocarbons contained in the stream. A noncondensed stream remaining after the condensation step, comprised predominantly of hydrogen and C1 to C3 hydrocarbons, is subjected to pressure swing adsorption or temperature swing adsorption at an adsorption temperature of about 0 DEG to about 250 DEG C. in a bed of adsorbent which selectively adsorbs ethylene and propylene, thereby adsorbing substantially all of the ethylene and propylene from the gas stream. The ethylene and/or propylene is recovered upon bed regeneration.
Description
The application is the part continuation application of 931129 U.S. SN that submit to, 159028 applications.
The present invention relates to cracking hydrocarbon, more specifically say it is from the tail gas of catalytic cracking process, to reclaim alkene.
The effluent of cracking hydrocarbon device contains the hydrocarbon of broad variety.In order to reclaim these hydrocarbon, with the effluent cooling and through a series of separating steps, for example condensation and distillation is so that reclaim heavy and light liquid composition.Reclaim after these components, remaining light gas stream can be with it compression and cooling, so the major part of hydrocarbon remaining in this air-flow is condensed.Remaining noncondensable gas (being commonly referred to as tail gas) mainly contains hydrogen and C-C hydrocarbon in a small amount behind this light gas compression and condensing steps, also may contain other gaseous fractions for example nitrogen and carbonic acid gas.Described tail gas is delivered to the torch or the usefulness that acts as a fuel usually.Be to make hydrocarbon remaining in the tail gas to reduce as far as possible, this light gas stream is tried one's best high pressure and is cooled to the low temperature of trying one's best by may being compressed to of implementing.Its result, for compression and cooling energy that light gas consumed rather considerable.
Therefore, urgent requirement is to make the C that reduces and make recovery from the total cost of the tail gas recycle cracked hydrocarbon product of hydrocarbon cracker
2And C
3The amount of alkene increases as far as possible.If have one from air-flow, to reclaim the effective of light alkene and have cost-benefit method, can achieve the above object.The invention provides a kind of alkene absorbing process, it can make hydrocarbon cracking processes process institute energy requirement reduce, and makes the contained light alkene of cracking unit tail gas reach basically recovery fully.
According to the present invention, with the hydrocarbon raw material cracking, the product that obtains comprises the mixture of lower hydrocarbon.The hydrocarbon component that is easy to condensation is separated from crackate earlier, and with the gaseous effluent compression and the cooling of remainder, thereby generation contains the condensation product of the hydrocarbon of additional content, and remaining is tail gas, its main hydrogeneous and C
1-C
3Hydrocarbon also may contain other gases such as nitrogen.Tail gas is delivered to alternating pressure (abbreviation transformation) absorbing process process (PSA), or alternating temperature-changing (abbreviation alternating temperature) absorbing process process (TSA), this process adopts temperature and the adsorbent bed that is higher than room temperature, this is these alkene of preferentially adsorbed from the air-flow that contains alkene and one or more alkane, the operational condition of adsorption process is to make not the gaseous fraction of absorption contain most of hydrogen contained in the tail gas and alkane component (if there is nitrogen, also comprise nitrogen), and be adsorbed component and contain most olefinic constituent contained in the tail gas stream.This technological process can advantageously all stay the alkene in this air-flow basically.
The general operational requirement(GOR) of this adsorption step is that about 0 ℃ to about 250 ℃ of temperature range preferably is higher than 50 ℃; The about 0.2-100 crust of working pressure (absolute pressure), preferably about 1-50 crust.
In a preferred version of the present invention, sorbent material is an A type zeolite, most preferably is with 4A type zeolite in the scheme.
When adopting the PSA absorbing process, be to use low pressure in regeneration step, pressure range (absolute pressure) is about 100-5000 millibar usually, is preferably about 100-2000 millibar.When adopting TSA technology, the bed tempertaure when regeneration of adsorbent beds is raised to about 100-350 ℃ usually, preferably about 150-300 ℃.
In another preferred version of the present invention, the regeneration of adsorption bed is adopted vacuum unit or is purged with following one or more: rare gas element, from the not adsorbed gas product of adsorption system or from the adsorbed gas product of adsorption system, perhaps adopt vacuum and purge regenerated and unite; And at least a portion of pressurizeing again of bed is by means of the desorption gas that is rich in alkene from adsorption system.
Accompanying drawing is a functional diagram, and expression is by the hydrocarbon cracking system of main embodiment of the present invention.
By main aspect of the present invention,, produce the gaseous product of mainly hydrogeneous and wide fraction hydro carbons with the hydrocarbon flow cracking.With this product cooling and fractionation, heavy hydrocarbon in the product and middle runnings are told.The hydrocarbon mixture of condensation is generally sent to further processing, reclaims various hydrocarbon-fraction sections and high purity hydro carbons from materials flow.The gas phase that stays after the condensing steps (is generally contained hydrogen, C
4And C
4Following hydrocarbon) condensable gas is told in compression, cooling and fractionation or flash distillation from materials flow.Incondensible part is mainly hydrogeneous, methane and a small amount of C
2-C
3Hydrocarbon is sent to PSA or TSA technological process with it, by this air-flow produce be rich in ethene, propylene absorption mutually and be rich in the not absorption phase of hydrogen and alkane (and nitrogen, if the words that exist).After the adsorption system desorption, the ethylene-propylene mixture is sent from this system, can be further purified or merges with above-mentioned condensable air-flow.
Can further understand the present invention by accompanying drawing.In the accompanying drawings, some do not illustrate for understanding the optional auxiliary facility of the present invention, for example compressor, heat exchanger, valve.
In the accompanying drawings, A represents hydrocarbon cracker, and B is a separation column, and C is a gas compressor, and D is a heat exchanger, and E is demethaniser or flasher, and F is the gas separation system of using adsorbent.
A can be the general any hydrocarbon cracking system that uses in the refining of petroleum, and used in the methods of the invention concrete cracking method does not constitute a part of the present invention, can adopt any thermally splitting commonly used and catalytic cracking process in the present invention.The entrance end of A generally is a hydrocarbon feed-pipe 2, and pneumatic outlet is through managing 4 inlets that are connected to separation column B after its cracking.B is conventional formula separation column, and its generation comprises C
4And C
4The top stream of following hydrocarbon comprises C
6And the side line product of heavier liquid hydrocarbon, and the bottom product that comprises the heavy residue component.These three kinds of products are discharged from tower B by pipe 6,8,10 respectively.Pipe 10 is by managing 12 inlets of receiving device A, and the overhead product of B links to each other with the inlet of device E through managing 6.On the pipe 6 compressor C and water cooler D are set.C and D can be compressor and the heat exchangers that is applicable to any GENERAL TYPE of compression, cooling appropriate hydrocarbon gas.E is any conventional formula flasher or separation column, and it is applicable to that the uncondensable tail gas that will send in the materials flow of this device separates with condensable light component wherein.The light hydrocarbon of condensation is discharged from E via pipe 14.The tail gas outlet of E is connected to separator F by pipe 16.
F is an adsorption system, and its major function is with from other gas delivery in the alkene in the tail gas of E (mainly being ethene, propylene) and this materials flow.This device generally is PSA or TSA system, wherein generally comprises the fixed bed of two or more a plurality of parallel settings, and be arranged to can the adsorption-desorption cyclical operation.In this system, adsorption bed flows out from adsorption system with false continuous mode to guarantee fulvene gas by stage circulation in turn.
The adsorption bed of F is filled with sorbent material, and it is adsorbs olefins from the mixed gas that contains alkene and one or more alkane optionally.Generally, sorbent used can be aluminum oxide, silicon oxide, zeolite, carbonaceous molecular sieve or the like.Typical case's sorbent material comprises aluminum oxide, silica gel, carbonaceous molecular sieve, zeolite such as A type and X type zeolite, y-type zeolite or the like.Preferred sorbent material is an A type zeolite, most preferably is 4A type zeolite.
4A type zeolite is the A type zeolite of na form, and its apparent pore size is about 3.6-4A.This kind sorbent material for high-temperature from ethene-ethane mixtures ethylene adsorption and from propylene-propane mixture adsorbs propylene have very highly selective and big capacity.This kind sorbent material is at its unmodified state that is when having only sodium ion as exchangeable cation, and it is the most effective being used for the present invention.Yet some character of this sorbent material such as heat-resisting and light fastness stability can be by being improved with a part of sodium ions of other cationic exchange.Therefore, comprise in preferred version of the present invention and use such 4A type zeolite that the sodium ion that some of them invest on the sorbent material is replaced by other metal ions, the ionic percentage that condition is exchanged is not too high so that make sorbent material lose its 4A type feature.The character that characterizes 4A type feature comprise this sorbent material high-temperature optionally from the ethylene-vinyl mixture ethylene adsorption and from propylene-propane mixture the ability of adsorbs propylene, and can be issued to above-mentioned purpose not causing in the mixture alkene that significant situation oligomeric or polymerization takes place.Generally speaking, determined that sodium ion can reach 25%(at most in equivalent in the 4A zeolite) can replace by exchange by other positively charged ions, and do not cause sorbent material to lose its 4A type feature.Comprise K, Ca, Mg, Sr, Zn, Co, Ag, Cu, Mn, Cd, Al, Ce or the like positively charged ion for being used for the positively charged ion that the isolating 4A zeolite of alkene-alkane can exchange.When with other cationic exchange sodium ions, preferably be less than about 10%(by equivalent) sodium ion replaced by other positively charged ions.The displacement sodium ion can improve the character of sorbent material.For example, replace the stability that some sodium ions can improve sorbent material with other positively charged ions.
Another kind of preferred sorbent material is that to contain some oxidizable metal cationic, for example contains copper adsorbent, and it has high loading capacity and the selectivity of preferentially adsorbed alkene from alkene-alkane gaseous mixture.The suitable adsorbent matrix that is used for the sorbent material of manufactured copper modification comprises silica gel and zeolite molecular sieve for example 4A type zeolite, 5A type zeolite, X type zeolite and y-type zeolite.Put down in writing manufacturing and the application and the suitable example that contains copper adsorbent of copper modified adsorbent in US4917711, the document is as the bibliography of this paper.
Separator F is provided with exhaust emission tube 18, purges tracheae 20 and alkene vent pipe 22, and in scheme shown in the drawings, it is connected to the light hydrocarbon vent pipe 14 of condensation.Purging back gas circulating tube 24 is connecting manages 22, and leads to the inlet of separator F.
By the technological process of system implementation shown in the accompanying drawing of the present invention, cracking is sent into cracking unit A with hydrocarbon feed such as gas oil.Usually its cracking becomes the pyritous gaseous product, and it is the mixture of hydrocarbon, and the hydrocarbon of for example maximum 12 carbon atoms also becomes the hydro carbons residue of heavy.The pyritous gaseous product leaves A, is separated into heavy residue then and discharges from managing 10 in separation column B, or leave native system, or be recycled to device A by managing 12.Discharge the intermediate hydrocarbons cuts via pipe 8, its major part is the liquid hydrocarbon of 5 or more carbon atoms; Also have the light hydrocarbon air-flow of discharging via pipe 6, its hydrocarbon mainly hydrogeneous and maximum 4 carbon atoms also may contain nitrogen.Light hydrocarbon in the pipe 6 is compressed to required pressure through device C, is cooled to wherein most of C in heat exchanger D
2-C
4The temperature of hydrocarbon condensation, and feeder E.Via the component of pipe 14 discharge easy condensation wherein from E, the processing unit (plant) of delivering to the downstream further separates various hydrocarbon.Mainly contain C via pipe 16 from the E discharge
1-C
3The air-flow of hydrocarbon is a tail gas, sends into separator F.
When the adsorption bed of tail gas by separator F, olefinic constituent wherein is adsorbed onto on the sorbent material, and hydrogen in this air-flow and alkane when existing (and nitrogen, if) pass through from adsorbent bed simultaneously, discharge i.e. not adsorbed gas from F via pipe 18.The preferred operations condition of separator F is with alkene all absorption basically, and the most of hydrogen and the alkane that will enter in the materials flow of this device are discharged.
The service temperature of absorption process depends on a number of factors, for example used concrete sorbent material, the 4A zeolite of for example unmodified 4A zeolite, specific metal exchange, or other can be from alkene-alkylating mixture other sorbent materials of selective adsorption alkene, also depend on the pressure when for example adsorbing.Generally, the minimum temperature of absorption process is about 0 ℃, about 50 ℃ of preferred minimum temperature, and most preferably temperature is to low about 70 ℃.The upper temperature limit that carries out absorption process among the F depends primarily on economic condition.Generally, the upper temperature limit of absorption process is for being lower than the temperature of alkene generation chemical reaction (as polyreaction).This upper temperature limit is about 250 ℃.When using unmodified 4A adsorbent of molecular sieve, usually or be lower than 200 ℃ and promptly react, preferred absorption process or be lower than 170 ℃ and carry out.The sorbent material that contains oxidizable metal, the sorbent material of copper modification for example, temperature be higher than about 100 ℃ effective especially, for example about 100-250 ℃.At the about 110-200 of temperature range ℃ of preferred these sorbent materials that use, most preferably be at the about 125-175 of temperature range ℃.
The pressure of PSA round-robin absorption process is generally about 0.2-100 crust, and preferably about 1-50 crust, TSA circulate and then be generally about normal pressure or high pressure more.
When adopting PSA technology, the temperature of step for regeneration temperature common and absorption process is approaching, and its absolute pressure is lower than adsorptive pressure.The pressure of the step for regeneration of PSA technology is about the 20-5000 millibar usually, preferred 100-2000 millibar.When implementing TSA technology, the bed regeneration temperature will be higher than adsorption temp, is generally about 100-350 ℃, is preferably about 150-300 ℃.When implementing TSA technology, the pressure of step for regeneration and absorption process is identical usually, and preferably two kinds of operations all adopt about normal pressure or high pressure more.When uniting employing PSA and TSA technology, the temperature and pressure of step for regeneration is respectively the temperature and pressure above and below absorption process.
In the container that is adsorbing of separator F, when being adsorbed the forward position and moving in this container desirable position of alkene, the absorption process in this container is stopped, enter step for regeneration.In when regeneration, container when PSA technology (if) that has adsorbed alkene is reduced pressure, perhaps when TSA technology (if) heat temperature raising.Along with regenerative process, the gas that is rich in alkene is discharged from separator F via pipe 20.This materials flow can merge (seeing accompanying drawing) with the light hydrocarbon materials flow of pipe 14, or system discharges for further processing thus.
The renovation process of adsorption bed depends on uses any absorbing process.For PSA technology, the regeneration stage generally includes adverse current step-down operation, makes an emptying with reflux type, until desirable low pressure.If need, pressure can be reduced under the barometric point by vacuum unit such as vacuum pump (not shown) in the bed.
Sometimes, except that above-mentioned adverse current step-down operation, may need to use one of air-flow that rare gas element or separator F discharge to purge adsorption bed.In the case, purge operation when beginning normally towards the end of above-mentioned adverse current step-down operation, or continue towards the there.During purging operation, can introduce the sweeping gas that can not adsorb to F via pipe 20, and with adverse current to passing through adsorption bed, thereby force alkene that desorption comes out to be discharged from F through managing 22, sweeping gas can be managed the 18 not gaseous products of absorption from the F discharge with process, perhaps with the gas that can not adsorb in other sources, for example inert permanent gases such as nitrogen.
By preferred method shown in the drawings, the alkene that F comes out at adverse current step-down operation institute desorption enters pipe 14, and sweep gas and be circulated back to F via pipe 24 at all or part of of the alkene that purges operation desorption from bed, reprocesses processing.The advantage of this embodiment is to make the amount of delivering to the sweeping gas in the pipe 14 reduce to minimum.
In sorption cycle, also comprise other operations outside absorption and these basic working procedure of regeneration.For example, make the adsorption bed step-down have benefit, the product of the first step-down operation can be used for other beds in the adsorption system are partly pressurizeed with multistep processes.The amount of the gas impurity that enters pipe 14 is further reduced.Comprise that in absorption phase with between the regeneration stage it also can be favourable that a following current purges operation.It is that the feed stream of sending into F is ended that described following current purges, and high purity olefin is sent into the adsorption bed that is in adsorptive pressure with concurrent simultaneously.Like this effect of making be force the room spatial that is among the F not adsorbed gas flow to the outlet of not adsorbed gas, thereby guarantee that the alkene that obtains has high purity when the adverse current step-down.The high purity olefin that is used for above-mentioned following current purging can derive from the process tank (not shown) of being located on the pipe 22, and this is meant when F only contains an adsorber; Perhaps from another adsorber that is in absorption phase, this is meant that F comprises a plurality of adsorbers arranged side by side and respectively according to the situation of stages operating mode.
Within the scope of the present invention, mode is to adopt conventional formula equipment to monitor and adjust automatically interior each gas flow of native system preferably, thereby can reach full-automatic operation continuously efficiently.
One of significant advantage of the present invention is to tell valuable alkene from the tail gas stream of hydrocarbon cracker, can not tell the alkane of contained lesser value in the tail gas too much simultaneously.Just this system can reach high selectivity, and therefore improves the overall recovery of alkene from the cracking technological process, and this is very helpful.
Further illustrate the present invention by following imaginary embodiment, wherein except that other person of indicating, umber, percentage ratio and ratio all are to be benchmark with the volume.This embodiment demonstrates the catalytic cracking that the inventive method is applied to gas oil.
Example 1
With fluidized bed catalytic cracker processing gasiform gas oil stream, catalyst system therefor is based on y-type zeolite and other active ingredients, and temperature is about 400 ℃, generates the materials flow of gasiform product.The gaseous product fractionation becomes: the heavy-gravity bottom product merges it charging gas oil with this catalytic cracking unit; The hydrocarbon mixture phlegma that side line obtains, it mainly contains C
5Heavier hydrocarbon, what obtain is liquid product; Also comprise the cat head gaseous stream, mainly contain C
4Reach more light-weight hydrocarbon.Top stream is compressed to pressure 33 crust, is cooled to 15 ℃ of temperature, send into the light hydrocarbon fractionation plant, this top stream of sending into is divided into the tower bottoms stream, it comprises most hydrocarbon, and cat head uncondensed gas stream, and its concentration data is listed in table 1(materials flow 1).
Above-mentioned uncooled air-flow is sent to the processing of PSA device, and this PSA technology has circulation in 2 minutes in adsorption system, and it comprises the contactor of a pair of filling 4A type zeolite, and they are parallel settings, respectively press stages operating.In absorption process, the adsorption bed temperature remains on 100 ℃, and pressure is 8 crust absolute pressure; In step for regeneration, pressure is reduced to 1.2 crust absolute pressure.The flow groups of the air-flow of desorption and not absorption is respectively in table 1, is respectively air-flow 2 and 3.
Table 1
Component air-flow 1 air-flow 2 air-flows 3
0.45kg/mol/hr 0.45kg-mol/hr 0.45kg-mol/hr
Hydrogen 178.8 17.9 160.9
Methane 955.8 372.7 583.0
Ethane 402.7 169.2 233.6
Ethene 209.6 167.7 41.9
Propylene 248.7 156.7 92.0
Propane 32.9 11.8 21.0
Trimethylmethane 2.0 0.0 2.1
1-butylene 2.0 0.0 2.0
Suitable-2-butylene 0.0 0.0 0.0
Normal butane 2.0 0.0 2.0
Isopentene 2.0 0.0 2.0
Positive amylene 2.0 0.0 2.0
Hexane 3.8 0.0 3.8
Amount to 2,043.4 898.0 1,149.3
Though the present invention is described with reference to concrete experiment, this experiment only is that the present invention is given an example, so other changes can be arranged.For example, the device layout of technological process of the present invention can be different from the accompanying drawing those shown.Scope of the present invention only is to be limited by the listed scope of claims.
Claims (26)
1, a kind of method that reclaims alkene, described alkene are selected from ethene, propylene and their mixture in the cracked hydrocarbon flow, and this method may further comprise the steps:
(a) from the cracked hydrocarbon product, tell a gaseous stream;
(b) with this gaseous stream cooling, become hydrocarbon flow and air-flow of condensation, the latter mainly comprises hydrogen and methane, and contains alkene in a small amount and the alkane that is selected from ethane, propane or its mixture;
(c) this air-flow is adopted the circulating adsorption process of adsorbent bed, this sorbent material is adsorbs olefins optionally, thus the component that is rich in alkene that obtains adsorbing and the component that is rich in hydrogen and alkane of absorption not; And
(d) with the described component that is rich in alkene desorption from the described sorbent material.
2, the method for claim 1 also comprises described gaseous stream compression.
3, the method for claim 1, described circulating adsorption process are to be selected from transformation absorption (PSA), alternating temperature absorption (TSA), perhaps both combined processes.
4, the absorption process that the process of claim 1 wherein is to carry out being higher than about 50 ℃ temperature.
5, the method for claim 4, absorption process wherein are to carry out in about 50-250 ℃ temperature range.
6, the method for claim 5, sorbent material wherein is to be selected from: aluminum oxide, 4A type zeolite, 5A type zeolite, 13X type zeolite, y-type zeolite, and these mixture.
7, the method for claim 6, sorbent material wherein contain can oxidation metal ion.
8, the method for claim 7, wherein said oxidable metal ion is a cupric ion.
9, the method for claim 8, absorption process wherein are to carry out in about 100-200 ℃ temperature range.
10, the method for claim 6, wherein said sorbent material are 4A type zeolites.
11, the method for claim 10, wherein said sorbent material comprise the tradable positively charged ion except that sodium ion, but its content is not enough so that this sorbent material loses its 4A type feature.
12, the method for claim 10, absorption process wherein are to carry out in about 50-200 ℃ temperature range and about 0.2-100 crust (absolute pressure) pressure range.
13, the method for claim 10, absorption process wherein are to carry out in about 70-170 ℃ temperature range and about 1-50 bar pressure scope.
14, claim 1 or 10 method, wherein said circulating adsorption process are transformation absorption (PSA), and the pressure during regeneration of adsorbent beds is about 20-5000 millibar (absolute pressure).
15, claim 1 or 10 method, wherein said circulating adsorption process are transformation absorption (TSA), and the temperature during regeneration of adsorbent beds is about 100-350 ℃.
16, the process of claim 1 wherein that described cracked hydrocarbon flow is produced by catalytic cracking.
17, the process of claim 1 wherein that described air-flow is to unite from the hydrocarbon flow of described condensation isolated by flash distillation, fractionation or the two.
18, the process of claim 1 wherein that the component that is rich in ethene and propylene of described desorption is that hydrocarbon flow with described condensation is merged together.
19, the method for claim 10, wherein said 4A type zeolite contains cupric ion, and step (d) is carried out in about 125-250 ℃ temperature range.
20, it is via adverse current step-down mode regenerated that the method for claim 10, wherein said 4A type zeolite have a part at least.
21, the method for claim 20, wherein said 4A type zeolite also are lower than barometric point and further regeneration through being depressurized to vacuum unit.
22, the method for claim 20, wherein said 4A type zeolite are also through with rare gas element, the not product gas of product gas, the desorption of absorption or their associating and further regeneration.
23, the process of claim 1 wherein that described alkene is ethene.
24, the method for claim 23, wherein said alkane is ethane.
25, the process of claim 1 wherein that described alkene is propylene.
26, the method for claim 25, wherein said alkane is propane.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US15902893A | 1993-11-29 | 1993-11-29 | |
| US159,028 | 1993-11-29 | ||
| US231,559 | 1994-04-22 | ||
| US08/231,559 US5744687A (en) | 1993-11-29 | 1994-04-22 | Process for recovering alkenes from cracked hydrocarbon streams |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1106055A true CN1106055A (en) | 1995-08-02 |
| CN1039428C CN1039428C (en) | 1998-08-05 |
Family
ID=26855593
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 94118602 Expired - Fee Related CN1039428C (en) | 1993-11-29 | 1994-11-29 | Catalytic cracking process |
Country Status (11)
| Country | Link |
|---|---|
| EP (1) | EP0655492B1 (en) |
| JP (1) | JP3566766B2 (en) |
| CN (1) | CN1039428C (en) |
| AU (1) | AU696774B2 (en) |
| CA (1) | CA2134821C (en) |
| DE (1) | DE69418830D1 (en) |
| NO (1) | NO309487B1 (en) |
| NZ (1) | NZ264809A (en) |
| PL (1) | PL178744B1 (en) |
| RU (1) | RU2100336C1 (en) |
| TR (1) | TR28172A (en) |
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| CN1048010C (en) * | 1995-10-24 | 2000-01-05 | 中国石油化工总公司 | Method for recovering ethene from dilute ethene-contg. gas |
| CN1309809C (en) * | 2002-10-08 | 2007-04-11 | 英国石油化学品有限公司 | Process for the removal of oxygen from olefin-containing process streams |
| CN1315763C (en) * | 2002-03-19 | 2007-05-16 | 埃克森美孚研究工程公司 | Separation of propylene from hydrocarbon mixtures |
| CN101486624A (en) * | 2009-02-19 | 2009-07-22 | 山东科技大学 | Complexing recycling process for dilute ethylene suspension bed |
| CN102778073A (en) * | 2012-08-10 | 2012-11-14 | 中石化广州工程有限公司 | Refrigerating device and process for recycling propylene by using waste heat and waste pressure in intensified gas fractionation device |
| CN105413386A (en) * | 2008-02-21 | 2016-03-23 | 埃克森美孚研究工程公司 | Separation Of Carbon Dioxide From Methane Utilizing Zeolitic Imidazolate Framework Materials |
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| CA2156582C (en) * | 1994-09-30 | 1999-01-26 | Raghu K. Menon | Hydrocarbon catalytic cracking process |
| US5856607A (en) * | 1996-05-03 | 1999-01-05 | Amoco Corporation | Process for production of ethylbenzene frome dilute ethylene streams |
| US6488741B2 (en) | 2001-01-23 | 2002-12-03 | The Trustess Of The University Of Pennsylvania | Light hydrocarbon separation using 8-member ring zeolites |
| DE102009012452A1 (en) * | 2009-03-12 | 2010-09-16 | Uhde Gmbh | A method for reducing olefin losses in the removal of carbon dioxide from an olefin stream from dehydrogenation reactions |
| WO2010123748A1 (en) * | 2009-04-24 | 2010-10-28 | Univation Technologies, Llc | Regeneration of purification beds with a jet compressor in an open loop cycle |
| KR101470675B1 (en) | 2010-08-26 | 2014-12-08 | 한국에너지기술연구원 | Displacement desorption process for light olefin separation |
| KR101270713B1 (en) * | 2010-08-26 | 2013-06-17 | 에스케이 주식회사 | Process for the recovery of ethylene from fcc off-gas |
| EP3040405A1 (en) * | 2014-12-30 | 2016-07-06 | Technip France | Method for improving propylene recovery from fluid catalytic cracker unit |
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| US3078636A (en) * | 1959-12-18 | 1963-02-26 | Union Carbide Corp | Unsaturated hydrocarbon separation |
| US4992601A (en) * | 1989-02-15 | 1991-02-12 | Energia Andina Ltd. | Process for the selective separation of alkenes and alkynes |
| EP0520672A3 (en) * | 1991-06-24 | 1993-06-16 | The Boc Group, Inc. | Method of removing gases and light hydrocarbons from gas streams |
| FI932187A (en) * | 1992-05-29 | 1993-11-30 | Boc Group Inc | FOERFARANDE FOER FRAMSTAELLNING AV OMAETTADE KOLVAETEN OCH SEPARERING AV DESAMMA FRAON MAETTADE KOLVAETEN |
| US5245099A (en) * | 1992-07-22 | 1993-09-14 | Uop | PSA process for recovery or ethylene |
-
1994
- 1994-10-27 NO NO944098A patent/NO309487B1/en not_active IP Right Cessation
- 1994-10-28 NZ NZ26480994A patent/NZ264809A/en not_active IP Right Cessation
- 1994-11-01 CA CA 2134821 patent/CA2134821C/en not_active Expired - Fee Related
- 1994-11-18 TR TR01188/94A patent/TR28172A/en unknown
- 1994-11-22 AU AU78972/94A patent/AU696774B2/en not_active Ceased
- 1994-11-23 RU RU94041683A patent/RU2100336C1/en not_active IP Right Cessation
- 1994-11-24 DE DE69418830T patent/DE69418830D1/en not_active Expired - Lifetime
- 1994-11-24 EP EP19940308703 patent/EP0655492B1/en not_active Expired - Lifetime
- 1994-11-28 PL PL94306025A patent/PL178744B1/en not_active IP Right Cessation
- 1994-11-29 CN CN 94118602 patent/CN1039428C/en not_active Expired - Fee Related
- 1994-11-29 JP JP29461694A patent/JP3566766B2/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1048010C (en) * | 1995-10-24 | 2000-01-05 | 中国石油化工总公司 | Method for recovering ethene from dilute ethene-contg. gas |
| CN1315763C (en) * | 2002-03-19 | 2007-05-16 | 埃克森美孚研究工程公司 | Separation of propylene from hydrocarbon mixtures |
| CN1309809C (en) * | 2002-10-08 | 2007-04-11 | 英国石油化学品有限公司 | Process for the removal of oxygen from olefin-containing process streams |
| CN105413386A (en) * | 2008-02-21 | 2016-03-23 | 埃克森美孚研究工程公司 | Separation Of Carbon Dioxide From Methane Utilizing Zeolitic Imidazolate Framework Materials |
| CN101486624A (en) * | 2009-02-19 | 2009-07-22 | 山东科技大学 | Complexing recycling process for dilute ethylene suspension bed |
| CN101486624B (en) * | 2009-02-19 | 2012-12-19 | 山东科技大学 | Complexing recycling process for dilute ethylene suspension bed |
| CN102778073A (en) * | 2012-08-10 | 2012-11-14 | 中石化广州工程有限公司 | Refrigerating device and process for recycling propylene by using waste heat and waste pressure in intensified gas fractionation device |
| CN102778073B (en) * | 2012-08-10 | 2015-03-25 | 中石化广州工程有限公司 | Refrigerating device and process for recycling propylene by using waste heat and waste pressure in intensified gas fractionation device |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2134821C (en) | 2000-05-16 |
| NO309487B1 (en) | 2001-02-05 |
| RU2100336C1 (en) | 1997-12-27 |
| RU94041683A (en) | 1996-10-10 |
| CA2134821A1 (en) | 1995-05-30 |
| AU696774B2 (en) | 1998-09-17 |
| NO944098D0 (en) | 1994-10-27 |
| PL178744B1 (en) | 2000-06-30 |
| EP0655492B1 (en) | 1999-06-02 |
| AU7897294A (en) | 1995-06-15 |
| JP3566766B2 (en) | 2004-09-15 |
| EP0655492A3 (en) | 1995-10-18 |
| PL306025A1 (en) | 1995-06-12 |
| TR28172A (en) | 1996-03-01 |
| NZ264809A (en) | 1996-10-28 |
| EP0655492A2 (en) | 1995-05-31 |
| JPH07207280A (en) | 1995-08-08 |
| NO944098L (en) | 1995-05-30 |
| DE69418830D1 (en) | 1999-07-08 |
| CN1039428C (en) | 1998-08-05 |
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