CN1159272C - Productive process for isoalkene and/or tertiary alkyl ether - Google Patents
Productive process for isoalkene and/or tertiary alkyl ether Download PDFInfo
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- CN1159272C CN1159272C CNB001340905A CN00134090A CN1159272C CN 1159272 C CN1159272 C CN 1159272C CN B001340905 A CNB001340905 A CN B001340905A CN 00134090 A CN00134090 A CN 00134090A CN 1159272 C CN1159272 C CN 1159272C
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Abstract
The present invention discloses a production process for isoolefine (tert-olefine) and/or tertiary alkyl ether. The present invention comprises the following steps: the separated light component fraction of low molecular weight ether is circulated into an ether synthesis reactor in order to inhibit side reaction in etherification reaction, and therefore, the utilization rate of alcohol in the system is enhanced. In the present invention, a water scrubbing tower used in the prior art is changed into a static mixer and a separation tank in order that device cost can be further saved.
Description
The present invention relates to the production technique of isoolefine (tertiary olefin) and/or tert-alkyl ether, particularly the technology of hydrocarbon mixture by containing a kind of isoolefine at least and at least a pure prepared in reaction high purity tert-alkyl ether or the hydrocarbon mixture by containing a kind of isoolefine at least and at least a pure prepared in reaction high purity tert-alkyl ether, prepare the technology of isoolefine by the cracking tert-alkyl ether again.
Tert-alkyl ether, isoolefine are the important source material of fine chemistry industry, also are the important intermediate raw material or the monomers of synthetic rubber, synthetic resins, are the raw material of preparing high-purity isoolefine as methyl tertiary butyl ether (MTBE), are again the important additives that improves fuel octane number; High-purity isobutylene is widely used in producing multiple Chemicals such as isoprene-isobutylene rubber, polyisobutene and methyl methacrylate.
When tert-alkyl ether is used for the different hydrocarbon alkene of preparing high-purity raw material, cracking technology has certain requirement to the purity of tert-alkyl ether, as the heavier content such as oligopolymer of isoolefine in the cracking stock more for a long time, can influence the activity of catalyst for cracking, simultaneously other hydrocarbon-fraction (particularly other alkene) content can influence the purity of the isoolefine that cracking obtains more for a long time in the cracking stock.With methyl tert-butyl ether cracking production high purity isoolefine is example, and its component concentration to cracking stock requires referring to table 1.
Table 1
| Chemical name | Be called for short | wt％ |
| Methyl tertiary butyl ether | MTBE | ＞99 |
| Methyl sec-butyl ether | MSBE | ＜0.5 |
| The mixed | C4 | ＜0.05 |
| Methyl alcohol | MeOH | ＜0.2 |
| The trimethyl carbinol | TBA | ＜0.5 |
| Diisobutylene | DIB | ＜0.1 |
| Water | H2O | No free-water |
Adopt the synthetic and cracking associating preparing high-purity isoolefine of tert-alkyl ether, have the reaction preference height, do not have advantages such as pollution and corrosion.Companies such as IFP (IFP), gondola Snamprogetti all carried out research to this, and had applied for a lot of patents.US 5,994,594 (1999,11,30) provide a kind of tert-alkyl ether to synthesize the process integration of uniting the preparing high-purity isoolefine with cracking, compared this technology with traditional technology and done some improvement, but still come with some shortcomings: use the middle and later periods at catalyzer, by product in the etherification reaction product hangs down molecule ether (ether that is formed by dehydration of alcohols) content and increases gradually, and promptly Chun selectivity descends gradually, has influenced pure utilization ratio.In addition, this patent still adopts traditional water wash column to remove the alcohol in the material after alcohol in the material behind the etherification reaction or the scission reaction, from improving the complicated operation degree, saves floor space and saves aspect such as cost of equipment and consider, also is further improved.
The object of the present invention is to provide a kind of production technique of improved tert-alkyl ether, adopt this technology can suppress by product generation, improve alcohol selectivity, reduce cost of equipment, save floor space and simplify the operation.
Another object of the present invention is to provide a kind of improved tert-alkyl ether and isoolefine process for combination producing, adopt this technology can suppress by product generation, improve alcohol selectivity, reduce cost of equipment, save floor space and simplify the operation.
For achieving the above object, the present invention also adopts and will contain low-molecular-weight ether lighting end and be circulated to etherification reaction zone, suppresses side reaction, especially uses the middle and later periods at catalyzer, makes alcohol keep higher selectivity, improves the utilization ratio of total system alcohol; Also that but prior art is the used water wash column of the present invention changes static mixer and separating tank into, with further reduction cost of equipment, save floor space and simplify the operation.
The invention provides the production technique of a kind of isoolefine and/or tert-alkyl ether, comprise that the hydrocarbon mixture and at least a alcohol that will contain a kind of isoolefine at least sends into etherification reaction zone R1, the product that will contain tert-alkyl ether from least a portion that etherification reaction zone obtains is sent into fractionation zone C1, to send into ether cracking zone R2 from least a portion high purity tert-alkyl ether product that fractionation zone C1 obtains, to send into from the product that contains isoolefine that ether cracking zone R2 makes and take off heavy separation column C3 or alcohol washing disengaging zone L2, the cut of isoolefine be will contain from least a portion that separation column C3 obtains or alcohol washing disengaging zone L2 or separation column C3 sent into respectively from the organic phase that at least a portion that alcohol washing disengaging zone L2 obtains contains isoolefine, to wash organic phase or the cut that at least a portion that disengaging zone L2 or separation column C3 obtain contains isoolefine from alcohol and send into separation column C4, obtain the high purity isoolefine and mainly contain the overhead fraction of lower molecular weight ether light constituent, it is characterized in that at least a portion is circulated to etherification reaction zone R1 from the overhead fraction that mainly contains lower molecular weight ether light constituent of separation column C4.
The present invention also provides the production technique of a kind of isoolefine and/or tert-alkyl ether, comprise that the hydrocarbon mixture and at least a alcohol that will contain a kind of isoolefine at least sends into etherification reaction zone R1, the product that will contain tert-alkyl ether from least a portion that etherification reaction zone obtains is sent into alcohol washing disengaging zone L1, to wash the organic phase that contains tert-alkyl ether that disengaging zone L1 obtains from alcohol and send into fractionation zone C1, to send into ether cracking zone R2 from least a portion high purity tert-alkyl ether product that fractionation zone C1 obtains, the product that will contain isoolefine from least a portion that ether cracking zone R2 makes is sent into and is taken off heavy separation column C3 or alcohol washing disengaging zone L2, the cut of isoolefine be will contain from least a portion that separation column C3 obtains or alcohol washing disengaging zone L2 or separation column C3 sent into respectively from the organic phase that at least a portion that alcohol washing disengaging zone L2 obtains contains isoolefine, to wash organic phase or the cut that at least a portion that disengaging zone L2 or separation column C3 obtain contains isoolefine from alcohol and send into separation column C4, obtain the high purity isoolefine and mainly contain the overhead fraction of lower molecular weight ether light constituent, it is characterized in that at least a portion is circulated to etherification reaction zone R1 from the overhead fraction that mainly contains lower molecular weight ether light constituent of separation column C4.
The present invention also provides the production technique of a kind of isoolefine and/or tert-alkyl ether, comprise that the hydrocarbon mixture and at least a alcohol that will contain a kind of isoolefine at least sends into etherification reaction zone R1, the product that will contain tert-alkyl ether from least a portion that etherification reaction zone obtains is sent into fractionation zone C1 or alcohol washing disengaging zone L1, to contain the unreacted hydrocarbon mixture from least a portion that fractionation zone C1 or alcohol washing disengaging zone L1 obtain, the cut of a small amount of lower molecular weight ether light constituent or organic phase are sent into alcohol washing disengaging zone L1 or fractionation zone C1, to wash at least a portion that disengaging zone L1 or fractionation zone C1 obtain from alcohol and contain the unreacted hydrocarbon mixture, the organic phase or the cut of a small amount of lower molecular weight ether light constituent are sent into separation column C2, the overhead fraction that obtains containing the tower bottom distillate of unreacted hydrocarbon mixture and mainly contain lower molecular weight ether light constituent is characterized in that at least a portion is circulated to etherification reaction zone R1 from the overhead fraction that mainly contains lower molecular weight ether light constituent of separation column C2.
Hydrocarbon material of the present invention contains at least a isoolefine (tertiary olefin), also contains component such as other saturated or unsaturated hydrocarbons, as the C from oil refining or petrochemical complex
4And/or C
5Material, C
4And/or C
5Steam cracking material (being generally the material of extraction behind the diene), all can be used as hydrocarbon material of the present invention from the material after isomerized catalytic pyrolysis material (hydrogenation isomerization and skeletal isomerization) and the paraffin dehydrogenation; Alcohol of the present invention mainly is the alcohol of 1-4 carbon atom, particular methanol and ethanol.The tert-alkyl ether of available prepared of the present invention is mainly methyl tertiary butyl ether (MTBE), Ethyl Tertisry Butyl Ether (ETBE), ethyl pentyl group ether (ETAE), tertiary amyl-methyl ether (TAME), sec.-propyl tertbutyl ether etc., the tertbutyl ether cracking obtains iso-butylene, the isoolefine that other tert-alkyl ether cracking obtains is a mixture, and cracking obtains 2-methyl-2-butene and 2-methyl-1-butene alkene mixture as TAME.The pure isoolefine that makes with the synthetic and cracking process integration of tert-alkyl ether of the present invention on one of them two key with the compound of branched-chain alkyl (methyl), these compounds are generally the isoolefine that contains 4-8 carbon atom, the isoolefine that preferably contains 4-6 carbon atom is as iso-butylene and isopentene, dissident's alkene, isooctene, isodecyl alkene etc.
The present invention adopts isolated low-molecular-weight ether lighting end is circulated to etherification reaction zone, to suppress the generation of by product lower molecular weight ether, improves the selectivity (especially when catalyzer turns round for a long time) of alcohol, thereby improves the utilization ratio of total system alcohol.
When prior art removes pure in the organic fraction, adopt water wash column, and the present invention adopts static mixer and separating tank, can further reduce cost of equipment, save floor space and simplify the operation.
Production technique below in conjunction with 1～15 pair of isoolefine of the present invention of accompanying drawing and/or tert-alkyl ether is further described.
Accompanying drawing 1～15th, the schematic flow sheet of isoolefine of the present invention and/or tert-alkyl ether production technique.The operation that dotted line representative in the accompanying drawing may exist, mean main containing of code name in the accompanying drawing:
R1-etherification reaction zone C1-fractionation zone
C2-separation column L1 alcohol washing disengaging zone
Mn-static mixer Vn-separating tank
R2-ether-splitting is separated reaction C3-separation column
L2 alcohol washing disengaging zone
Mm-static mixer Vm-separating tank
C5-separation column C4-separation column
The invention provides the production technology (referring to accompanying drawing 1) of a kind of isoalkene and/or tert-alkyl ether, comprise the hydrocarbon mixture that will contain at least a kind of isoalkene and at least a alcohol respectively through pipeline 1,2 and 2a send into the etherification reaction zone R1 that catalyst for etherification is housed, contained at least a kind of product P 1 of tert-alkyl ether. To send into fractionation zone C1 by at least a portion etherification product P1 that etherification reaction zone R1 obtains, mainly contained the organic fraction O1 of unreacted hydrocarbon mixture, unreacting alcohol, a small amount of low-molecular-weight ether light component (low-molecular-weight ether is formed by dehydration of alcohols) and the fraction B 1 that mainly contains the tert-alkyl ether cut, recombinates and divide, this fractionation zone contains at least one fractionating column, can satisfy the requirement of cracking with the tert-alkyl ether of guaranteeing gained, organic fraction O1 can be used as Organic Chemicals or liquefied gas etc., also can further separate and can also be partly recirculated to etherification reaction zone R1, preferably further separates. The part of the high-purity tert-alkyl ether fraction B 1 of gained can be used as fuel additive, industrial chemicals, another part high-purity tert-alkyl ether fraction B 1 is sent into the ether-splitting solution reaction zone R2 that ether-splitting solution catalyst is housed, obtain containing the product P 2 of at least a isoalkene and at least a alcohol. The ether-splitting solution product P 2 that will obtain from ether-splitting solution reaction zone R2 is delivered to fractionating column C3, mainly contained the cut O4 of isoalkene, pure and mild low-molecular-weight ether light component (low-molecular-weight ether is formed by dehydration of alcohols) and contained alcohol, the fraction B 4 of cracking tert-alkyl ether not, the fraction B 4 that at least a portion is contained pure and mild not cracking tert-alkyl ether is back to etherification reaction zone R1, another part B4 cut is sent into the ether storage tank, can be used as fuel additive, the cut O4 that mainly contains isoalkene, pure and mild low-molecular-weight ether light component can be used as industrial chemicals or is used for further refining. To send into from least a portion overhead fraction O4 of fractionating column C3 alcohol washing Disengagement zone L2, fresh water is sent into alcohol washing Disengagement zone L2 through pipeline 4, obtains mainly moisture, pure aqueous phase B 5 and mainly contains the organic phase O5 of isoalkene, a small amount of low-molecular-weight ether light component. Described alcohol washing Disengagement zone L2 selects at least one water scrubber T2 or at least one group of static mixer Mm and knockout drum Vm. From reduce cost of equipment, save floor space, the angle that simplifies the operation considers the alcohol washing preferred static mixer in Disengagement zone of the present invention and knockout drum. Mainly moisture, pure aqueous phase B 5 can be sent into the waste water treatment plant or further separate to reclaim alcohol; The organic phase O5 that mainly contains isoalkene, a small amount of low-molecular-weight ether light component can be used as Organic Chemicals or liquefied gas etc., also can further separate to obtain the high-purity isoalkene. To wash the organic phase O5 that at least a portion that the Disengagement zone obtains mainly contains isoalkene, a small amount of low-molecular-weight ether light component from alcohol and send into fractionating column C4, at the bottom of tower, obtain highly purified isoalkene fraction B 7, can be used as monomer or the industrial chemicals of polymer; The light component cut O7 that mainly contains low molecule ether that obtains from cat head is circulated to etherification reaction zone R1, can suppress like this generation of the low molecule ether of accessory substance, improves the utilization rate of alcohol.
For unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component are separated with alcohol, the production technology of isoalkene of the present invention and/or tert-alkyl ether also comprises alcohol washing Disengagement zone L1 (referring to accompanying drawing 3) when etherification reaction zone R1, fractionation zone C1, ether-splitting solution reaction zone R2, fractionating column C3, alcohol washing Disengagement zone L2 and fractionating column C4 exist, to send into from least a portion overhead fraction O1 that fractionation zone C1 obtains alcohol washing Disengagement zone L1, fresh water W1 sends into alcohol washing Disengagement zone L1 through pipeline 3, obtains mainly moisture, pure aqueous phase B 2 and mainly contains the organic phase O2 of unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component. Described alcohol washing Disengagement zone L1 selects at least one water scrubber T1 or at least one group of static mixer Mn and knockout drum Vn. From reduce cost of equipment, save floor space, the angle that simplifies the operation considers the alcohol washing preferred static mixer in Disengagement zone of the present invention and knockout drum. Mainly moisture, pure aqueous phase B 2 can be sent into the waste water treatment plant or further separate to reclaim alcohol; The organic phase O2 that mainly contains unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component can be used as Organic Chemicals or liquefied gas etc., also can further separate so that the unreacted hydrocarbon mixture separates with low-molecular-weight ether, alcohol can also be washed the part organic phase O2 that Disengagement zone L1 obtains and be circulated to etherification reaction zone R1, can suppress like this generation of the low molecule ether of accessory substance, improve the utilization rate of alcohol, preferably further separate.
For further light component among the organic phase O2 being separated with the unreacted hydrocarbon mixture, the production technology of isoalkene of the present invention and/or tert-alkyl ether also comprises fractionating column C2 (referring to accompanying drawing 3) when etherification reaction zone R1, fractionation zone C1, alcohol washing Disengagement zone L1, ether-splitting solution reaction zone R2, fractionating column C3, alcohol washing Disengagement zone L2 and fractionating column C4 exist, to wash the organic phase O2 that at least a portion that the Disengagement zone obtains mainly contains unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component from alcohol and send into fractionating column C2, and mainly be contained the light component cut O3 of low molecule ether and mainly contain unreacted hydrocarbon mixture B3 cut. Cut O3 or discharge or be circulated to etherification reaction zone R1 preferably are circulated to etherification reaction zone R1 with cut O3, can suppress like this generation of the low molecule ether of accessory substance, improve the utilization rate of alcohol.
In order further to reclaim the alcohol that contains in the pure aqueous distillate, the production technology of isoalkene of the present invention and/or tert-alkyl ether also comprises alcohol recovery fractionating column C5 (referring to accompanying drawing 3) at alcohol washing Disengagement zone L1 and/or pure the washing when Disengagement zone L2 exists, to send into alcohol from containing of pure moisture abscission zone L1 of pure aqueous phase B 2 and reclaim fractionating column C5, and/or from containing of pure moisture abscission zone L2 pure aqueous phase B 5 send into alcohol and reclaim fractionating column C5, with aqueous distillate B6 and the rich pure cut O6 that obtains poor alcohol. The rich pure cut O6 that at least a portion cat head is obtained is circulated to etherification reaction zone R1, and aqueous distillate B6 is circulated to alcohol washing Disengagement zone L1 and/or washing Disengagement zone L2 at the bottom of at least a portion tower, also water at the bottom of the tower of a small amount of fractionating column C5 can be discharged. When alcohol washing Disengagement zone L1 and/or alcohol washing Disengagement zone L2 use recycle-water (recirculated water), also can wash Disengagement zone L1 and/or alcohol washing Disengagement zone L2 adds a part of fresh water W1 and/or W2 to alcohol.
The isoalkene purifying of gained also can adopt the method (referring to accompanying drawing 2, accompanying drawing 4) of washing first aftercut after the ether-splitting solution of the production technology of isoalkene of the present invention and/or tert-alkyl ether, itself and the synthetic main distinction with cracking process integration (accompanying drawing 1, accompanying drawing 3) of above-mentioned tert-alkyl ether are: the ether-splitting product P 2 from the ether cracking zone is introduced into alcohol washing Disengagement zone L2, obtain moisture, pure aqueous phase B 5 and contain cracking tert-alkyl ether not, isoalkene, a small amount of organic phase O5a of low molecule ether light component, organic phase O5a from alcohol washing Disengagement zone L2 enters fractionating column C3, mainly contained the cut O4a of isoalkene and low-molecular-weight ether and mainly contained the not fraction B 4a of cracking tert-alkyl ether, at least a portion overhead fraction O4a of fractionating column C3 enters fractionating column C4 tower, at least a portion contains mainly not that the fraction B 4a of cracking tert-alkyl ether is circulated to ether-splitting solution reaction zone R2, and the flow direction of other cut is synthetic identical with the cracking process integration with above-mentioned tert-alkyl ether.
The invention provides the production technology (referring to accompanying drawing 5) of a kind of isoalkene and/or tert-alkyl ether, comprise that hydrocarbon mixture and at least a alcohol that will contain at least a kind of isoalkene sends into the etherification reaction zone R1 that catalyst for etherification is housed through pipeline 1,2 respectively, contained at least a kind of product P 1 of tert-alkyl ether. To obtain at least a portion etherification product P1 by etherification reaction zone R1 and send into alcohol washing Disengagement zone L1, fresh water W1 sends into alcohol washing Disengagement zone L1 through pipeline 3, obtains mainly moisture, pure aqueous phase B 2 and mainly contains the organic phase O2a of tert-alkyl ether, unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component. Described alcohol washing Disengagement zone L1 selects at least one water scrubber T1 or at least one group of static mixer Mn and knockout drum Vn. From reduce cost of equipment, save floor space, the angle that simplifies the operation considers the alcohol washing preferred static mixer in Disengagement zone of the present invention and knockout drum. Mainly moisture, pure aqueous phase B 2 can be sent into the waste water treatment plant or further separate to reclaim alcohol. The organic phase O2a that at least a portion is mainly contained tert-alkyl ether, unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component sends into fractionation zone C1, mainly contained the organic fraction O1a of unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component and the fraction B 1 that mainly contains the tert-alkyl ether cut, recombinates and divide, this fractionation zone contains at least one fractionating column, can satisfy the requirement of cracking with the tert-alkyl ether of guaranteeing gained, organic fraction O1a can be used as Organic Chemicals or liquefied gas etc., also can further separate, can also partly be circulated to etherification reaction zone R1, preferably further separate. Can be with the part of the high-purity tert-alkyl ether fraction B 1 of gained as fuel additive, industrial chemicals, at least a portion high-purity tert-alkyl ether fraction B 1 is sent into the ether-splitting solution reaction zone R2 that ether-splitting solution catalyst is housed, obtain containing the product P 2 of at least a isoalkene and at least a alcohol. The ether-splitting solution product P 2 that will obtain from ether-splitting solution reaction zone R2 is delivered to fractionating column C3, mainly contained the cut O4 of isoalkene, pure and mild low-molecular-weight ether light component and contained the fraction B 4 of pure and mild not cracking tert-alkyl ether, the fraction B 4 that at least a portion is contained pure and mild not cracking tert-alkyl ether is back to etherification reaction zone R1, another part B4 cut is sent into the ether storage tank, can be used as fuel additive; The cut O4 that mainly contains isoalkene, pure and mild low-molecular-weight ether light component can be used as industrial chemicals or is used for further refining. At least a portion is sent into alcohol washing Disengagement zone L2 from the overhead fraction O4 of fractionating column C3, fresh water is sent into alcohol washing Disengagement zone L2 through pipeline 4, obtains mainly moisture, pure aqueous phase B 5 and mainly contains the organic phase O5 of isoalkene, a small amount of low-molecular-weight ether light component. Described alcohol washing Disengagement zone L2 selects at least one water scrubber T2 or at least one group of static mixer Mm and knockout drum Vm. From reduce cost of equipment, save floor space, the angle that simplifies the operation considers the alcohol washing preferred static mixer in Disengagement zone of the present invention and knockout drum. Mainly moisture, pure aqueous phase B 5 can be sent into the waste water treatment plant or further separate to reclaim alcohol; The organic phase O5 that mainly contains isoalkene, a small amount of low-molecular-weight ether light component can be used as Organic Chemicals or liquefied gas etc., also can further separate to obtain purer isoalkene. The organic phase O5 that at least a portion is mainly contained isoalkene, a small amount of low-molecular-weight ether light component from alcohol washing Disengagement zone sends into fractionating column C4, obtains highly purified isoalkene B7 at the bottom of tower, can be used as monomer or the industrial chemicals of polymer; At least a portion that obtains from cat head mainly contains low molecule ether light component O7 and is circulated to etherification reaction zone R1, can suppress like this generation of the low molecule ether of accessory substance, improves the utilization rate of alcohol.
For further light component among the organic fraction O1a being separated with the unreacted hydrocarbon mixture, the production technology of isoalkene of the present invention and/or tert-alkyl ether also comprises fractionating column C2 (referring to accompanying drawing 7) when etherification reaction zone R1, alcohol washing Disengagement zone L1, fractionation zone C1, ether-splitting solution reaction zone R2, fractionating column C3, alcohol washing Disengagement zone L2 and fractionating column C4 exist, to obtain the organic fraction O1a that at least a portion mainly contains unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component from fractionation zone C1 and send into fractionating column C2, mainly contained the light component cut O3 of low molecule ether and mainly contained unreacted hydrocarbon mixture B3 cut, overhead fraction O3 can make industrial chemicals or further separate or be circulated to etherification reaction zone R1, preferably overhead fraction O3 is circulated to etherification reaction zone R1, can suppress like this generation of the low molecule ether of accessory substance, improve the utilization rate of alcohol.
In order further to reclaim the alcohol that contains in the pure aqueous distillate, the production technology of isoalkene of the present invention and/or tert-alkyl ether comprises that also alcohol reclaims fractionating column C5 (referring to accompanying drawing 7) when alcohol washing Disengagement zone L1 exists with alcohol washing Disengagement zone L2, to send into alcohol from containing of pure moisture abscission zone L1 of pure aqueous phase B 2 and reclaim fractionating column C5, and/or from containing of pure moisture abscission zone L2 pure aqueous phase B 5 send into alcohol and reclaim fractionating column C5, with aqueous distillate B6 and the rich pure cut O6 that obtains poor alcohol. The rich pure cut O6 that cat head obtains is circulated to etherification reaction zone R1, and aqueous distillate B6 is circulated to alcohol washing Disengagement zone L1 and/or washing Disengagement zone L2 at the bottom of at least a portion tower, also water at the bottom of the tower of a small amount of fractionating column C5 can be discharged. When alcohol washing Disengagement zone L1 and/or alcohol washing Disengagement zone L2 use recycle-water (recirculated water), also can wash Disengagement zone L1 and/or alcohol washing Disengagement zone L2 adds a part of fresh water W1 and/or W2 to alcohol.
The isoalkene purifying of gained also can adopt the method (referring to accompanying drawing 6, accompanying drawing 8) of washing first aftercut after the ether-splitting solution of the production technology of isoalkene of the present invention and/or tert-alkyl ether, itself and the synthetic main distinction with cracking process integration (accompanying drawing 5, accompanying drawing 7) of above-mentioned tert-alkyl ether are: the ether-splitting product P 2 from the ether cracking zone is introduced into alcohol washing Disengagement zone L2, obtain moisture, pure aqueous phase B 5 and contain cracking tert-alkyl ether not, isoalkene, a small amount of organic phase O5a of low molecule ether light component, at least a portion organic phase O5a from alcohol washing Disengagement zone L2 enters fractionating column C3, mainly contained the cut O4a of isoalkene and low-molecular-weight ether and mainly contained the not fraction B 4a of cracking tert-alkyl ether, at least a portion overhead fraction O4a of fractionating column C3 enters fractionating column C4 tower, contain mainly not that the fraction B 4a of cracking tert-alkyl ether is circulated to ether-splitting solution reaction zone R2, the flow direction of other cut is synthetic identical with the cracking process integration with above-mentioned tert-alkyl ether.
The invention provides the production technology (referring to accompanying drawing 9) of a kind of isoalkene and/or tert-alkyl ether, comprise the hydrocarbon mixture that will contain at least a kind of isoalkene and at least a alcohol respectively through pipeline 1,2 and 2a send into the etherification reaction zone R1 that catalyst for etherification is housed, contained at least a kind of product P 1 of tert-alkyl ether. To obtain at least a portion etherification product P1 by etherification reaction zone R1 and send into fractionation zone C1, mainly contained the organic fraction O1 of unreacted hydrocarbon mixture, unreacting alcohol, a small amount of low-molecular-weight ether light component and mainly contained the tert-alkyl ether cut and restructuring minute cut B1, this fractionation zone contains at least one fractionating column, in order to obtain satisfying the tert-alkyl ether of the requirement of cracking. Organic fraction O1 can be used as Organic Chemicals or liquefied gas etc., also can further separate, and can also be partly recirculated to etherification reaction zone R1, preferably further separates. The part of the tert-alkyl ether fraction B 1 of gained can be used as fuel additive, industrial chemicals, also can further separate, to obtain the high-purity tert-alkyl ether. To send into from least a portion overhead fraction O1 that fractionation zone C1 obtains alcohol washing Disengagement zone L1, and obtain mainly moisture, pure aqueous phase B 2 and mainly contain the organic phase O2 of unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component. Described alcohol washing Disengagement zone L1 selects at least one water scrubber T1 (referring to Figure 11) or at least one group of static mixer Mm and knockout drum Vm (referring to Fig. 9,12). From reduce cost of equipment, save floor space, the angle that simplifies the operation considers the alcohol washing preferred static mixer in Disengagement zone of the present invention and knockout drum. Mainly moisture, pure aqueous phase B 2 can be sent into the waste water treatment plant or further separate to reclaim alcohol; The organic phase O2 that mainly contains unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component can be used as Organic Chemicals or liquefied gas etc., also can further separate so that the unreacted hydrocarbon mixture separates with low-molecular-weight ether, alcohol can also be washed the part organic phase O2 that Disengagement zone L1 obtains and be circulated to etherification reaction zone R1, can suppress like this generation of the low molecule ether of accessory substance, improve the utilization rate of alcohol, preferably further separate. To wash the organic phase O2 that at least a portion that the Disengagement zone obtains mainly contains unreacted hydrocarbon mixture, a small amount of low-molecular-weight ether light component from alcohol and send into fractionating column C2, mainly contained the light component cut O3 of low molecule ether and mainly contained unreacted hydrocarbon mixture fraction B 3, the at least a portion that obtains from cat head mainly contains low molecule ether light component and is circulated to etherification reaction zone R1, can suppress like this generation of the low molecule ether of accessory substance, improve the utilization rate of alcohol.
In order further to reclaim the alcohol that contains in the pure aqueous distillate, the production technique of isoolefine of the present invention and/or tert-alkyl ether comprises that also alcohol reclaims separation column C5 (referring to accompanying drawing 9) when etherification reaction zone R1, fractionation zone C1, alcohol washing disengaging zone L1 and separation column C2 exist, to contain pure aqueous phase B 2 from least a portion of pure moisture abscission zone L1 and send into alcohol recovery separation column C5, with aqueous distillate B6 and the rich pure cut O6 that obtains poor alcohol.The rich pure cut O6 that cat head obtains is circulated to etherification reaction zone R1, and aqueous distillate B6 is circulated to alcohol washing disengaging zone L1 and/or washing disengaging zone L2 at the bottom of at least one the tower, and water can be discharged at the bottom of the tower of a spot of separation column C5.
The purifying of the tert-alkyl ether product of the synthetic back of the ether of the production technique of isoolefine of the present invention and/or tert-alkyl ether gained also can adopt the method (referring to accompanying drawing 10) of washing aftercut earlier, itself and the synthetic key distinction with cracking process integration (accompanying drawing 9) of above-mentioned tert-alkyl ether are: the product P 1 from etherification reaction zone R1 is introduced into alcohol washing disengaging zone L1, obtains mainly moisture, pure aqueous phase B 2 and mainly contains the organic phase O2a of tert-alkyl ether, unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent.Mainly moisture, pure aqueous phase B 2 can be sent into the waste water treatment plant or further handle to reclaim alcohol.The organic fraction O2a that at least a portion is mainly contained tert-alkyl ether, unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent sends into fractionation zone C1, mainly contained the organic phase O1a of unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent and mainly contained the fraction B 1 of tert-alkyl ether cut, heavy constituent, this fractionation zone C1 contains at least one separation column, with at least a portion contain cracking tert-alkyl ether not, isoolefine, the cut O1a of low molecule ether light constituent sends into separation column C2 on a small quantity, the flow direction of other cut is identical with above-mentioned tert-alkyl ether synthesis technique.
The operational condition of the production technique of preparation isoolefine of the present invention and/or tert-alkyl ether is as described below: etherification reaction zone R1, at least the reaction raw materials that contains a kind of hydrocarbon mixture of isoolefine and contain a kind of alcohol is at least sent into etherification reaction zone R1, and etherification reaction zone comprises at least one methyltertiarvbutyl ether reactor.The methyltertiarvbutyl ether reactor that prior art is announced all can be used for the present invention, as can be simple catalyticreactor, also can be the catalytic distillation reactor.Catalyst for etherification can be disclosed any catalyzer that can be used for the isoolefine etherificate in the prior art, as an acidic catalyst (being generally the solid acid catalyst that forms by organic acid acetic) and mineral acid ester catalyst, the present invention preferentially selects solid acid resin catalyzer such as Amberlyst 15 or 35 (this catalyzer can be bought from the market) for use, the range of reaction temperature of methyltertiarvbutyl ether reactor R1 is 30 ℃～100 ℃, preferable range is 40 ℃～90 ℃, pressure range is 0.1～4.0MPa, preferred pressure range is 0.1～2.5MPa, and the air speed scope of methyltertiarvbutyl ether reactor is 0.01～50hr
-1, preferable range is 0.1～10hr
-1The alcohol that enters this methyltertiarvbutyl ether reactor can be the reuse alcohol from pure recovery tower C5, can be fresh alcohol also, and the alcohol that enters this methyltertiarvbutyl ether reactor is 0.3～5.0 with the scope that contains the hydrocarbon mixture weight ratio of isoolefine, and preferable range is 0.5～3.0.
The operational condition of fractionation zone C1 is as follows: fractionation zone C1 selects at least one separation column for use, and the working pressure scope of separation column is at 0.1～3.0MPa, and preferable range is 0.5～2.0MPa, and the number of theoretical plate of this tower is between 3～80, and preferable range is between 10～50.
The condition that ether-splitting is separated reaction zone R2 is as follows: ether-splitting is separated reaction zone and is comprised that at least one ether-splitting separates reactor, and the methyltertiarvbutyl ether reactor that prior art is announced all can be used for the present invention.Catalyst for etherification can be disclosed any ether cracked catalyzer that can be used in the prior art, preferably select solid acid catalyst for use, the present invention preferentially selects loading type inorganic acid salt catalyzer for use, this catalyzer is to adopt the described method of GB1173128 patent to make, its acid quality generally is controlled at 20%～30%, the reaction pressure that this ether-splitting is separated reactor is controlled between 0.1～3.0MPa, preferable range is between 0.1～1.2MPa, temperature of reaction is between 50 ℃～300 ℃, preferable range is between 100 ℃～250 ℃, and this ether-splitting is separated the air speed of reactor at 0.5～50h
-1Between, preferable range is at 1～10h
-1Between.
The operational condition of separation column C3 is as follows: the working pressure scope of this separation column is at 0.1～1.5MPa, and preferable range is 0.1～1.0MPa, and the number of theoretical plate of this tower is between 3～80, and preferable range is between 10～50.
Alcohol washing disengaging zone L1 operational condition is as follows: the organic fraction that enters this washing disengaging zone is 0.005～20 with the weight ratio that enters this disengaging zone water, and preferable range is between 0.01～5.The working pressure of this washing disengaging zone is between 0.1～2.0MPa, and preferable range is between 0.1～1.5MPa, and service temperature is 10 ℃～60 ℃.
The operational condition of alcohol washing disengaging zone L2 is as follows: containing pure cut is 0.005～20 with entering this disengaging zone water weight ratio, and preferable range is between 0.01～5.The working pressure of this washing disengaging zone is between 0.1～2.0MPa, and preferable range is between 0.1～1.5MPa, and service temperature is 10 ℃～60 ℃.
The operational condition of separation column C5 is as follows: the working pressure of this separation column is between 0.1～1.2MPa, and preferable range is between 0.1～0.8MPa, and number of theoretical plate is between 3～80, and preferable range is between 10～50.
The operational condition of separation column C2 is as follows: the working pressure of this separation column is between 0.1～1.2MPa, and preferable range is between 0.1～0.8MPa, and number of theoretical plate is between 3～80, and preferable range is between 5～50.
The operational condition of separation column C4 is as follows: the working pressure of this separation column is between 0.1～1.5MPa, and preferable range is between 0.3～1.0MPa, and number of theoretical plate is between 3～80, and preferable range is between 5～50.
Further specify the present invention below in conjunction with embodiment, but do not limit to its scope.
Embodiments of the invention with methyl tertiary butyl ether synthetic with pure iso-butylene of cracking legal system (IB) and pure methyl-tert butylene (MTBE) be that example illustrates production technique of the present invention.Wherein to separate the catalyzer of reactor charge be solid acid catalyst to ether-splitting, is to adopt the described method preparation of GB1173128 patent, and concrete preparation method is as follows: flood γ-Al with aluminum sulfate aqueous solution
2O
3, its after drying also was prepared from 450 ℃ of roastings in 3 hours, and the content of sulfate radical is 20% (weight percent) on the catalyzer.
The mixed c 4 hydrocarbon that contains iso-butylene (removes the cracking c_4 raw material behind the diene, down with) and methyl alcohol enter methyltertiarvbutyl ether reactor R1 through pipeline 1,2 and 2a respectively, the content of iso-butylene is about 20% (weight) in the mixed c 4 hydrocarbon, the material quantity that enters methyltertiarvbutyl ether reactor is 100kg/h, and Amberlyst 15 solid acid resin catalyzer (ROHM ﹠amp are housed among the methyltertiarvbutyl ether reactor R1; HAAS produces), 60 ℃ of the temperature of reaction of methyltertiarvbutyl ether reactor R1, reaction pressure are 1.2MPa, the air speed 6hr of methyltertiarvbutyl ether reactor
-1Entering the methyl alcohol of this methyltertiarvbutyl ether reactor and the weight ratio of iso-butylene is 0.6.Etherification product P1 enters the separation column C1a in the C1 fractionation zone, separation column C1a cat head obtains the O1 cut, the B1a cut that obtains at the bottom of the tower enters separation column C1b, separation column C1b is mainly contained the B1 cut of methyl tertiary butyl ether, obtain the B2 cut at the bottom of the tower, the working pressure of separation column C1a is 0.9MPa, the number of theoretical plate of this tower is 25, the working pressure of separation column C1b is 1.3MPa, the number of theoretical plate of this tower is 30, the overhead fraction B1 of separation column C1b enters ether-splitting and separates reactor R2, and it is solid acid catalyst that catalyst for etherification is housed among the reactor R2, and this catalyzer is to adopt the described method of GB1173128 patent to make, its sulfate radical content is 20%, the reaction pressure that this ether-splitting is separated reactor is 0.55MPa, and temperature of reaction is at 200 ℃, reaction velocity 2h
-1Between, separate the product P 2 that reactor obtains from ether-splitting and enter separation column C3, the working pressure of separation column C3 is 0.8MPa, number of theoretical plate is 25, the overhead fraction O4 of separation column C3 enters alcohol washing disengaging zone L2, two static mixers and two separating tanks (separating tank is the horizontal tank of band baffle plate) are adopted in this washing disengaging zone, the working pressure of two groups of static mixers and separating tank is 0.6Mpa, service temperature is 40 ℃, fresh water is respectively through pipeline 4,4a enters static mixer (Mm1, Mm2), enter static mixer (Mm1, Mm2) organic fraction O4, Oa1 and fresh water (W2, W2a) weight ratio is respectively 0.5,0.4, isolated organic fraction O5 enters separation column C4 from separating tank, the working pressure of separation column C 4 is 0.7MPa, number of theoretical plate is 35, separation column C4 overhead fraction O7 sends methyltertiarvbutyl ether reactor R1 back to, obtain purity at the bottom of the fractionation Tata and be 99.93% iso-butylene, this product can be used as the monomer of polymerization product, its technical process is referring to Figure 12, and table 2～table 4 has provided the mass flow of each equipment of turnover in this technical process.
Table 2
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1a cat head O1 cut (kg/h) | B1a cut (kg/h) at the bottom of the C1a tower | B2 cut (kg/h) at the bottom of the C1b tower | |
| H 2O | 0.03 | 0.03 | 0.03 | ||
| IB | 19.97 | 3.10 | 3.10 | ||
| All the other C4 | 68.10 | 68.10 | 68.10 | ||
| MeOH | 12.02 | 2.41 | 2.41 | ||
| MTBE | 26.20 | 26.20 | 0.09 | ||
| MSBE | 0.01 | 0.01 | |||
| DME * | 0.03 | 0.09 | 0.09 | ||
| TBA | 0.09 | 0.04 | 0.05 | ||
| DIB | 0.12 | 0.12 | 0.11 | ||
| Add up to | 100.15 | 100.15 | 73.77 | 26.38 | 0.20 |
*The DME-----dme
Table 3
| C1b cat head B1 cut (kg/h) | R2 exports P2 cut (kg/h) | C3 cat head O4 cut (kg/h) | B4 cut (kg/h) at the bottom of the C3 tower | The Mm1 W2 (kg/h) of intaking | |
| H 2O | 0.06 | 0.01 | 0.05 | 7.80 | |
| IB | 14.81 | 14.81 | |||
| All the other C4 | 0.01 | 0.01 | 0.01 | ||
| MeOH | 8.29 | 0.67 | 7.62 | ||
| MTBE | 26.11 | 2.85 | 2.85 | ||
| MSBE | 0.01 | 0.01 | 0.01 | ||
| DME | 0.10 | 0.10 | |||
| TBA | 0.05 | 0.02 | 0.02 | ||
| DIB | 0.01 | 0.03 | 0.03 | ||
| Add up to | 26.18 | 26.18 | 15.60 | 10.58 | 7.80 |
Table 4
| The Mm2 W2 (kg/h) of intaking | Vm2 exports organic phase O5 (kg/h) | C4 cat head O7 cut (kg/h) | B7 cut (kg/h) at the bottom of the C4 tower | |
| H 2O | 6.24 | 0.01 | 0.01 | |
| IB | 14.81 | 0.21 | 14.60 | |
| All the other C4 | 0.01 | 0.01 | ||
| MeOH | ||||
| MTBE | ||||
| MSBE | ||||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | ||||
| Add up to | 6.24 | 14.88 | 0.27 | 14.61 |
Comparative Examples 1
Substantially with embodiment 1, just the overhead fraction O7 of separation column C4 does not return methyltertiarvbutyl ether reactor R1, be in the accompanying drawing 12 not with the return wire of fractionator overhead to methyltertiarvbutyl ether reactor R1, other is with embodiment 1, table 5～table 7 has provided the mass flow of each equipment of turnover in this technical process.Table 8 has provided the interior technology of the present invention of certain hour and traditional technology optionally influences methyl alcohol in this system.
Table 5
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1a cat head O1 cut (kg/h) | B1a cut (kg/h) at the bottom of the C1a tower | B2 cut (kg/h) at the bottom of the C1b tower | |
| H 2O | 0.03 | 0.04 | 0.04 | ||
| IB | 19.85 | 3.08 | 3.08 | ||
| All the other C4 | 68.10 | 68.10 | 68.09 | 0.01 | |
| MeOH | 12.02 | 2.43 | 2.43 | ||
| MTBE | 26.05 | 26.05 | 0.09 | ||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.09 | 0.09 | |||
| TBA | 0.09 | 0.04 | 0.05 | ||
| DIB | 0.11 | 0.11 | 0.10 | ||
| Add up to | 100.00 | 100.00 | 73.77 | 26.23 | 0.19 |
Table 6
| C1b cat head B1 cut (kg/h) | R2 exports P2 cut (kg/h) | C3 cat head O4 cut (kg/h) | B4 cut (kg/h) at the bottom of the C3 tower | The Mm1 W2 (kg/h) of intaking | |
| H 2O | 0.06 | 0.01 | 0.05 | 7.77 | |
| IB | 14.77 | 14.77 | |||
| All the other C4 | 0.01 | 0.01 | 0.01 | ||
| MeOH | 8.23 | 0.66 | 7.57 | ||
| MTBE | 25.96 | 2.82 | 2.82 | ||
| MSBE | 0.01 | 0.01 | 0.01 | ||
| DME | 0.09 | 0.09 | |||
| TBA | 0.05 | 0.02 | 0.02 | ||
| DIB | 0.01 | 0.03 | 0.03 | ||
| Add up to | 26.04 | 26.04 | 15.54 | 10.50 | 7.77 |
Table 7
| The Mm2 W2 (kg/h) of intaking | Vm2 exports organic phase O5 (kg/h) | C4 cat head O7 cut (kg/h) | B7 cut (kg/h) at the bottom of the C4 tower | |
| H 2O | 6.22 | 0.01 | 0.01 | |
| IB | 14.77 | 0.18 | 14.59 | |
| All the other C4 | 0.01 | 0.01 | ||
| MeOH | ||||
| MTBE | ||||
| MSBE | ||||
| DME | 0.04 | 0.04 | ||
| TBA | ||||
| DIB | ||||
| Add up to | 6.22 | 14.83 | 0.23 | 14.60 |
Table 8
| Technology of the present invention (embodiment 1) | Traditional technology (Comparative Examples 1) | ||
| Methyl alcohol selectivity (%) | The etherification reaction time (0～6 month) | 99 | 99 |
| The etherification reaction time (7 months) | 99 | 98 | |
From table 2～table 8 as can be seen, set up the return wire of separation column C4 overhead fraction O7, can suppress the generation of the side reaction thing (dme) in the etherification reaction, improve the selectivity of methyl alcohol, promptly improve the utilization ratio of the methyl alcohol in the total system to methyltertiarvbutyl ether reactor R1.
The mixed c 4 hydrocarbon and the methyl alcohol that contain iso-butylene enter methyltertiarvbutyl ether reactor R1 through pipeline 1,2 and 2a respectively, the content of iso-butylene is about 20% (weight) in the mixed c 4 hydrocarbon, the material quantity that enters methyltertiarvbutyl ether reactor is 100kg/h, the catalyzer of loading among the methyltertiarvbutyl ether reactor R1 and the operational condition of reactor are with embodiment 1, and entering the methyl alcohol of this methyltertiarvbutyl ether reactor and the weight ratio of iso-butylene is 0.6.Etherificate product P 1 cut that obtains enters the separation column C1a in the C1 fractionation zone, separation column C1a cat head obtains the O1 cut, the B1a cut that obtains at the bottom of the tower enters separation column C1b, the B1 cut that separation column C1b is mainly contained methyl tertiary butyl ether enters ether-splitting and separates reactor R2, the catalyzer that reactor R2 loads and the operational condition of reactor are with embodiment 1, separate product P 2 cuts that reactor obtains from ether-splitting and enter alcohol washing disengaging zone L2, two static mixers and two separating tanks are adopted in this washing disengaging zone, the operational condition of two groups of static mixers and separating tank is with embodiment 1, fresh water is respectively through pipeline 4,4a enters static mixer (Mm1, Mm2), enter static mixer (Mm1, Mm2) organic fraction O4, Oa1 and fresh water (W2, W2a) weight ratio is respectively 2.0,1.0, isolated organic phase O5a enters separation column C3 from separating tank (Vm2), separation column C3 overhead fraction O4a enters separation column C4, separation column C4 overhead fraction O7 sends methyltertiarvbutyl ether reactor R1 back to, obtain purity at the bottom of the separation column C4 tower and be 99.93% iso-butylene, its technical process is referring to Figure 13, the operational condition of major equipment is with embodiment 1, and table 9～table 11 has provided the mass flow of each equipment of turnover in this technical process.
Table 9
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1a cat head O1 cut (kg/h) | B1a cut (kg/h) at the bottom of the C1a tower | C1b cat head B1 cut (kg/h) | |
| H 2O | 0.03 | 0.03 | 0.03 | ||
| IB | 19.97 | 3.10 | 3.10 | ||
| All the other C4 | 68.10 | 68.10 | 68.09 | 0.01 | |
| MeOH | 12.02 | 2.41 | 2.41 | ||
| MTBE | 26.20 | 26.20 | 26.11 | ||
| MSBE | 0.01 | 0.01 | 0.01 | ||
| DME | 0.03 | 0.09 | 0.09 | ||
| TBA | 0.09 | 0.04 | 0.05 | 0.05 | |
| DIB | 0.12 | 0.12 | 0.01 | ||
| Add up to | 100.15 | 100.15 | 73.77 | 26.38 | 26.18 |
Table 10
| B2 cut (kg/h) at the bottom of the C1b tower | R2 exports P2 cut (kg/h) | The Mm1 W2 (kg/h) of intaking | The Mm2 W2a (kg/h) of intaking | Vm2 exports organic phase O5a (kg/h) | |
| H 2O | 0.06 | 25.36 | 26.18 | 0.02 | |
| IB | 14.81 | 14.81 | |||
| All the other C4 | 0.01 | 0.01 | |||
| MeOH | 8.29 | ||||
| MTBE | 0.09 | 2.85 | 2.85 | ||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.10 | 0.05 | |||
| TBA | 0.02 | ||||
| DIB | 0.11 | 0.03 | 25.36 | 25.36 | 0.03 |
| Add up to | 0.20 | 26.18 | 52.36 | 26.18 | 17.78 |
Table 11
| C3 cat head O4a cut (kg/h) | B4a cut (kg/h) at the bottom of the C3 tower | C4 cat head O7 cut (kg/h) | B7 cut (kg/h) at the bottom of the C4 tower | |
| H 2O | 0.02 | |||
| IB | 14.81 | 0.21 | 14.10 | |
| All the other C4 | 0.01 | 0.01 | ||
| MeOH | ||||
| MTBE | 2.85 | |||
| MSBE | 0.01 | |||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | 0.03 | |||
| Add up to | 14.87 | 2.91 | 0.26 | 14.61 |
Comparative Examples 2
Substantially with embodiment 2, just the overhead fraction O7 of separation column C4 does not return methyltertiarvbutyl ether reactor R1, be in the accompanying drawing 13 not with the return wire of fractionator overhead to methyltertiarvbutyl ether reactor R1, other is with embodiment 2, table 12～table 14 has provided the mass flow of each equipment of turnover in this technical process.
Table 12
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1a cat head O1 cut (kg/h) | B1a cut (kg/h) at the bottom of the C1a tower | C1b cat head B1 cut (kg/h) | |
| H 2O | 0.03 | 0.04 | 0.04 | ||
| IB | 19.85 | 3.08 | 3.08 | ||
| All the other C4 | 68.10 | 68.10 | 68.09 | 0.01 | 0.01 |
| MeOH | 12.02 | 2.43 | 2.43 | ||
| MTBE | 26.05 | 26.05 | 25.96 | ||
| MSBE | 0.01 | 0.01 | 0.01 | ||
| DME | 0.09 | ||||
| TBA | 0.09 | 0.05 | 0.05 | ||
| DIB | 0.11 | 0.11 | 0.01 | ||
| Add up to | 100.00 | 100.00 | 73.77 | 26.23 | 26.04 |
Table 13
| B2 cut (kg/h) at the bottom of the C1b tower | R2 exports P2 cut (kg/h) | The Mm1 W2 (kg/h) of intaking | The Mm2 W2a (kg/h) of intaking | Vm2 exports organic phase O5a (kg/h) | |
| H 2O | 0.06 | 52.08 | 26.04 | 0.02 | |
| IB | 14.77 | 14.77 | |||
| All the other C4 | 0.01 | 0.01 | |||
| MeOH | 8.23 | ||||
| MTBE | 0.09 | 2.82 | 2.82 | ||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.09 | 0.05 | |||
| TBA | 0.02 | ||||
| DIB | 0.10 | 0.03 | 0.03 | ||
| Add up to | 0.19 | 26.04 | 52.08 | 26.04 | 17.71 |
Table 14
| C3 cat head O4a cut (kg/h) | B4a cut (kg/h) at the bottom of the C3 tower | C4 cat head O7 cut (kg/h) | B7 cut (kg/h) at the bottom of the C4 tower | |
| H 2O | 0.02 | |||
| IB | 14.77 | 0.20 | 14.57 | |
| All the other C4 | 0.01 | 0.01 | ||
| MeOH | ||||
| MTBE | 2.82 | |||
| MSBE | 0.01 | |||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | 0.03 | |||
| Add up to | 14.83 | 2.88 | 0.25 | 14.58 |
Set up the return wire of separation column C4 overhead fraction O7 among the embodiment 2, also obtain the result of table 8 among the embodiment 1 to methyltertiarvbutyl ether reactor R1.
The mixed c 4 hydrocarbon and the methyl alcohol that contain iso-butylene enter methyltertiarvbutyl ether reactor R1 through pipeline 1,2 and 2a respectively, the content of iso-butylene is about 20% (weight) in the mixed c 4 hydrocarbon, the material quantity that enters methyltertiarvbutyl ether reactor is 100kg/h, the catalyzer of loading among the methyltertiarvbutyl ether reactor R1 and the operational condition of reactor are with embodiment 1, and entering the methyl alcohol of this methyltertiarvbutyl ether reactor and the weight ratio of iso-butylene is 0.6.Etherificate product P 1 cut that obtains enters alcohol washing disengaging zone L1, washing disengaging zone L1 adopts two static mixers and two separating tanks (separating tank is the horizontal tank of band baffle plate), the working pressure of static mixer and separating tank is 0.6Mpa, service temperature is 40 ℃, fresh water is respectively through pipeline 3,3a enters static mixer (Mn1, Mn2), enter static mixer (Mn1, Mn2) organic fraction P1, O ' and fresh water (W1, W1a) weight ratio is respectively 0.5,0.4, enter separation column C1a the C1 fractionation zone from the isolated organic fraction O2a of separating tank (Vn2), separation column C1a cat head obtains the O1a cut, the B1a cut that obtains at the bottom of the tower enters separation column C1b, the B1 cut that separation column C1b is mainly contained methyl tertiary butyl ether enters ether-splitting and separates reactor R2, the catalyzer that reactor R2 loads and the operational condition of reactor are with embodiment 1, separate the product P 2 that reactor obtains from ether-splitting and enter separation column C3, the overhead fraction O4 of separation column C3 enters alcohol washing disengaging zone L2, two static mixers and two separating tanks are adopted in this washing disengaging zone, fresh water is respectively through pipeline 4,4a enters static mixer (Mm1, Mm2), enter static mixer (Mm1, Mm2) organic fraction O4, Oa1 and fresh water (W2, W2a) weight ratio is respectively 0.5,0.4, isolated organic fraction O5 enters separation column C4 from separating tank, separation column C4 overhead fraction O7 sends methyltertiarvbutyl ether reactor R1 back to, obtaining purity at the bottom of the fractionation Tata is 99.93% iso-butylene, its technical process is referring to Figure 14, except that the operational condition of aforesaid device and embodiment 1 are different, the operational condition of miscellaneous equipment is with embodiment 1, and table 15～table 17 has provided the mass flow of each equipment of turnover in this technical process.
Table 15
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | The Mn1 W1 (kg/h) of intaking | The Mn1 W1a (kg/h) of intaking | Vn2 exports organic phase O2a (kg/h) | C1a cat head O1a cut (kg/h) | |
| H 2O | 0.03 | 0.04 | 50.08 | 40.06 | 0.02 | 0.02 |
| IB | 19.97 | 3.10 | 3.10 | 3.10 | ||
| All the other C4 | 68.10 | 68.10 | 68.10 | 68.09 | ||
| MeOH | 12.02 | 2.41 | ||||
| MTBE | 26.20 | 26.20 | ||||
| MSBE | 0.01 | 0.01 | ||||
| DME | 0.03 | 0.09 | 0.05 | 0.05 | ||
| TBA | 0.09 | |||||
| DIB | 0.11 | 0.11 | ||||
| Add up to | 100.15 | 100.15 | 50.08 | 40.06 | 97.59 | 71.26 |
Table 16
| B1a cut (kg/h) at the bottom of the C1a tower | C1b cat head B1 cut (kg/h) | B2 cut (kg/h) at the bottom of the C1b tower | R2 exports P2 cut (kg/h) | C3 cat head O4 cut (kg/h) | B4 cut (kg/h) at the bottom of the C3 tower | |
| H 2O | 0.05 | 0.01 | 0.04 | |||
| IB | 14.82 | 14.82 | ||||
| All the other C4 | 0.01 | 0.01 | 0.01 | 0.01 | ||
| MeOH | 8.28 | 0.66 | 7.62 | |||
| MTBE | 26.20 | 26.11 | 0.09 | 2.84 | 2.84 | |
| MSBE | 0.01 | 0.01 | 0.01 | 0.01 | ||
| DME | 0.10 | 0.10 | ||||
| TBA | ||||||
| DIB | 0.11 | 0.01 | 0.10 | 0.03 | 0.03 | |
| Add up to | 26.33 | 26.14 | 0.19 | 26.14 | 15.60 | 10.54 |
Table 17
| The Mm1 W2 (kg/h) of intaking | The Mm1 W2 (kg/h) of intaking | Vm2 exports organic phase O5 (kg/h) | C4 cat head O7 cut (kg/h) | B7 cut (kg/h) at the bottom of the C4 tower | |
| H 2O | 7.80 | 6.24 | 0.02 | 0.02 | |
| IB | 14.82 | 0.18 | 14.64 | ||
| All the other C4 | 0.01 | 0.01 | |||
| MeOH | |||||
| MTBE | |||||
| MSBE | |||||
| DME | 0.05 | 0.05 | |||
| TBA | |||||
| DIB | |||||
| Add up to | 7.80 | 6.24 | 14.90 | 0.25 | 14.05 |
Comparative Examples 3
Substantially with embodiment 3, just the overhead fraction O7 of separation column C4 does not return methyltertiarvbutyl ether reactor R1, be in the accompanying drawing 14 not with the return wire of fractionator overhead to methyltertiarvbutyl ether reactor R1, other is with embodiment 3, table 18～table 20 has provided the mass flow of each equipment of turnover in this technical process.
Table 18
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | The Mn1 W1 (kg/h) of intaking | The Mn1 W1a (kg/h) of intaking | Vn2 exports organic phase O2a (kg/h) | C1a cat head O1a cut (kg/h) | |
| H 2O | 0.03 | 0.04 | 50.00 | 40.00 | 0.02 | 0.02 |
| IB | 19.85 | 3.08 | 3.08 | 3.08 | ||
| All the other C4 | 68.10 | 68.10 | 68.10 | 68.09 | ||
| MeOH | 12.02 | 2.43 | ||||
| MTBE | 26.05 | 26.05 | ||||
| MSBE | 0.01 | 0.01 | ||||
| DME | 0.09 | 0.05 | 0.05 | |||
| TBA | 0.09 | |||||
| DIB | 0.11 | 0.11 | ||||
| Add up to | 100.00 | 100.00 | 50.00 | 40.00 | 97.42 | 71.24 |
Table 19
| B1a cut (kg/h) at the bottom of the C1a tower | C1b cat head B1 cut (kg/h) | B2 cut (kg/h) at the bottom of the C1b tower | R2 exports P2 cut (kg/h) | C3 cat head O4 cut (kg/h) | B4 cut (kg/h) at the bottom of the C3 tower | |
| H 2O | 0.05 | 0.01 | 0.04 | |||
| IB | 14.73 | 14.73 | ||||
| All the other C4 | 0.01 | 0.01 | 0.01 | 0.01 | ||
| MeOH | 8.24 | 0.66 | 7.58 | |||
| MTBE | 26.05 | 25.96 | 0.09 | 2.83 | 2.83 | |
| MSBE | 0.01 | 0.01 | 0.01 | 0.01 | ||
| DME | 0.09 | 0.09 | ||||
| TBA | ||||||
| DIB | 0.11 | 0.01 | 0.10 | 0.03 | 0.03 | |
| Add up to | 26.18 | 25.99 | 0.19 | 25.99 | 15.50 | 10.49 |
Table 20
| The Mm1 W2 (kg/h) of intaking | The Mm1 W2 (kg/h) of intaking | Vm2 exports O5 cut (kg/h) | C4 cat head O7 cut (kg/h) | B7 cut (kg/h) at the bottom of the C4 tower | |
| H 2O | 7.75 | 6.20 | 0.02 | 0.02 | |
| IB | 14.73 | 0.19 | 14.54 | ||
| All the other C4 | 0.01 | 0.01 | |||
| MeOH | |||||
| MTBE | |||||
| MSBE | |||||
| DME | 0.05 | 0.05 | |||
| TBA | |||||
| DIB | |||||
| Add up to | 7.75 | 6.20 | 14.81 | 0.26 | 14.55 |
Set up the return wire of separation column C4 overhead fraction O7 among the embodiment 3, also obtain the result of table 8 among the embodiment 1 to methyltertiarvbutyl ether reactor R1.
The mixed c 4 hydrocarbon and the methyl alcohol that contain iso-butylene enter methyltertiarvbutyl ether reactor R1 through pipeline 1,2 and 2a respectively, the content of iso-butylene is about 20% (weight) in the mixed c 4 hydrocarbon, the material quantity that enters methyltertiarvbutyl ether reactor is 100kg/h, and the catalyzer that methyltertiarvbutyl ether reactor R1 loads and the operational condition of reactor are with embodiment 1.Entering the methyl alcohol of this methyltertiarvbutyl ether reactor and the weight ratio of iso-butylene is 0.6.Etherificate product P 1 cut enters separation column C1, can obtain purity at the bottom of the fractionation Tata is 99.20% methyl tertiary butyl ether (MTBE), MTBE can make fuel dope, also can make to prepare the raw material of high-purity isobutylene, but need further to purify, the overhead fraction O1 of separation column C1 enters alcohol washing disengaging zone L1, washing disengaging zone L1 adopts two static mixers and two separating tanks (separating tank is the horizontal tank of band baffle plate), the working pressure of static mixer and separating tank is 0.6Mpa, service temperature is 40 ℃, fresh water is respectively through pipeline 3,3a enters static mixer (Mn1, Mn2), enter static mixer (Mn1, Mn2) organic fraction O1, O ' and fresh water (W1, W1a) weight ratio is respectively 0.5,0.4, enter separation column C2 from the isolated organic fraction O2 of separating tank Vn2, the working pressure of separation column C2 is 0.7Mpa, number of theoretical plate is 25, separation column C2 overhead fraction O3 sends methyltertiarvbutyl ether reactor R1 back to, obtain unreacted C-4-fraction at the bottom of the fractionation Tata, its concrete technical process is referring to Figure 15, and table 21 and table 22 have provided the mass flow of each equipment of turnover in this technical process.
Table 21
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1 cat head O1 cut (kg/h) | B1 cut (kg/h) at the bottom of the C1 tower | The Mn1 W1 (kg/h) of intaking | |
| H 2O | 0.04 | 0.05 | 0.04 | 0.01 | 36.97 |
| IB | 19.86 | 3.09 | 3.09 | ||
| All the other C4 | 68.25 | 68.25 | 68.23 | 0.02 | |
| MeOH | 12.02 | 2.42 | 2.42 | ||
| MTBE | 26.07 | 26.07 | |||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.04 | 0.11 | 0.11 | ||
| TBA | 0.09 | 0.04 | 0.05 | ||
| DIB | 0.1 2 | 0.12 | |||
| Add up to | 100.21 | 100.21 | 73.93 | 26.28 | 36.97 |
Table 22
| The Mn2 W1a (kg/h) of intaking | Vn2 exports organic phase O2 (kg/h) | C2 cat head O3 cut (kg/h) | B3 cut (kg/h) at the bottom of the C2 tower | |
| H 2O | 29.57 | 0.04 | 0.02 | 0.02 |
| IB | 3.09 | 0.01 | 3.08 | |
| All the other C4 | 68.23 | 0.16 | 68.07 | |
| MeOH | ||||
| MTBE | ||||
| MSBE | ||||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | ||||
| Add up to | 29.57 | 71.41 | 0.24 | 71.17 |
Comparative Examples 4
Substantially with embodiment 4, just the overhead fraction O7 of separation column C4 does not return methyltertiarvbutyl ether reactor R1, be in the accompanying drawing 15 not with the return wire of fractionator overhead to methyltertiarvbutyl ether reactor R1, other is with embodiment 4, table 23 and table 24 have provided the mass flow of each equipment of turnover in this technical process.
Table 23
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1 cat head O1 cut (kg/h) | B1 cut (kg/h) at the bottom of the C1 tower | The Mn1 W1 (kg/h) of intaking | |
| H 2O | 0.03 | 0.04 | 0.04 | 36.89 | |
| IB | 19.85 | 3.08 | 3.08 | ||
| All the other C4 | 68.10 | 68.10 | 68.09 | 0.01 | |
| MeOH | 12.02 | 2.43 | 2.43 | ||
| MTBE | 26.05 | 26.05 | |||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.09 | 0.09 | |||
| TBA | 0.09 | 0.04 | 0.05 | ||
| DIB | 0.11 | 0.11 | |||
| Add up to | 100.00 | 100.00 | 73.77 | 26.23 | 36.89 |
Table 24
| The Mn2 W1a (kg/h) of intaking | Vn2 exports organic phase O2 (kg/h) | C2 cat head O3 cut (kg/h) | B3 cut (kg/h) at the bottom of the C2 tower | |
| H 2O | 29.51 | 0.04 | 0.02 | 0.02 |
| IB | 3.08 | 0.01 | 3.07 | |
| All the other C4 | 68.09 | 0.16 | 67.93 | |
| MeOH | ||||
| MTBE | ||||
| MSBE | ||||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | ||||
| Add up to | 29.51 | 71.26 | 0.24 | 71.02 |
Set up the return wire of separation column C2 overhead fraction O3 among the embodiment 4, also obtain the result of table 8 among the embodiment 1 to methyltertiarvbutyl ether reactor R1.
Embodiment 5
The mixed c 4 hydrocarbon and the methyl alcohol that contain iso-butylene enter methyltertiarvbutyl ether reactor R1 through pipeline 1,2 and 2a respectively, the content of iso-butylene is about 20% (weight) in the mixed c 4 hydrocarbon, the material quantity that enters methyltertiarvbutyl ether reactor is 100kg/h, and the catalyzer that methyltertiarvbutyl ether reactor R1 loads and the operational condition of reactor are with embodiment 1.Entering the methyl alcohol of this methyltertiarvbutyl ether reactor and the weight ratio of iso-butylene is 0.6.Etherificate product P 1 cut enters separation column C1, the overhead fraction O1 of separation column C1 enters alcohol washing disengaging zone L1, alcohol washing disengaging zone L1 adopts a water wash column T1, the working pressure of water wash column is 0.6Mpa, service temperature is 40 ℃, fresh water enters water wash column through pipeline 3, the weight ratio that enters the cut O1 of water wash column and fresh water is for O.9, water wash column cat head organic phase O2 enters separation column C2, separation column C2 overhead fraction O3 sends methyltertiarvbutyl ether reactor R1 back to, the operational condition of separation column C2 is with embodiment 4, obtain C-4-fraction at the bottom of the fractionation Tata, its technical process is referring to Figure 11, the separation column C5 of this example among Fig. 9, other is with embodiment 5, and table 25 and table 26 have provided the mass flow of each equipment of turnover in this technical process.
Table 25
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1 cat head O1 cut (kg/h) | B1 cut (kg/h) at the bottom of the C1 tower | The Mn1 W1 (kg/h) of intaking | |
| H 2O | 0.04 | 0.05 | 0.04 | 0.01 | 36.97 |
| IB | 19.86 | 3.08 | 3.08 | ||
| All the other C4 | 68.25 | 68.25 | 68.23 | 0.02 | |
| MeOH | 12.02 | 2.41 | 2.41 | ||
| MTBE | 26.11 | 26.11 | |||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.04 | 0.10 | 0.10 | ||
| TBA | 0.08 | 0.04 | 0.04 | ||
| DIB | 0.12 | 0.12 | |||
| Add up to | 100.21 | 100.21 | 73.90 | 26.31 | 36.97 |
Table 26
| The Mn2 W1a (kg/h) of intaking | Vn2 exports organic phase O2 (kg/h) | C2 cat head O3 cut (kg/h) | B3 cut (kg/h) at the bottom of the C2 tower | |
| H 2O | 29.57 | 0.04 | 0.02 | 0.02 |
| IB | 3.08 | 0.01 | 3.07 | |
| All the other C4 | 68.23 | 0.16 | 68.07 | |
| Me3H | ||||
| MTBE | ||||
| MSBE | ||||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | ||||
| Add up to | 29.57 | 71.40 | 0.24 | 71.16 |
Comparative Examples 5
Substantially with embodiment 5, just the overhead fraction O3 of separation column C2 does not return methyltertiarvbutyl ether reactor R1, be not with the return wire of fractionator overhead in the accompanying drawing 11 to methyltertiarvbutyl ether reactor R1, other is substantially with embodiment 5, table 27 and table 28 have provided the mass flow of each equipment of turnover in this technical process, adopt production technique of the present invention as and if cracking associating preparing high-purity iso-butylene production equipment synthetic at 3.5 ten thousand tons of/year MTBE, promptly replace water wash column with two groups of static mixers and separating tank, its cost of equipment relatively sees Table 29.
Table 27
| The R1 cut (kg/h) that enters the mouth | R1 exports P1 cut (kg/h) | C1 cat head O1 cut (kg/h) | B1 cut (kg/h) at the bottom of the C1 tower | The Mn1 W1 (kg/h) of intaking | |
| H 2O | 0.03 | 0.04 | 0.04 | 36.89 | |
| IB | 19.85 | 3.09 | 3.09 | ||
| All the other C4 | 68.10 | 68.10 | 68.09 | 0.01 | |
| MeOH | 12.02 | 2.44 | 2.44 | ||
| MTBE | 26.03 | 26.03 | |||
| MSBE | 0.01 | 0.01 | |||
| DME | 0.09 | 0.09 | |||
| TBA | 0.09 | 0.04 | 0.05 | ||
| DIB | 0.11 | 0.11 | |||
| Add up to | 100.00 | 100.00 | 73.79 | 26.21 | 36.89 |
Table 28
| The Mn2 W1a (kg/h) of intaking | Vn2 exports organic phase O2 (kg/h) | C2 cat head O3 cut (kg/h) | B3 cut (kg/h) at the bottom of the C2 tower | |
| H 2O | 29.51 | 0.04 | 0.02 | 0.02 |
| IB | 3.09 | 0.01 | 3.08 | |
| All the other C4 | 68.09 | 0.16 | 67.93 | |
| MeOH | ||||
| MTBE | ||||
| MSBE | ||||
| DME | 0.05 | 0.05 | ||
| TBA | ||||
| DIB | ||||
| Add up to | 29.51 | 71.27 | 0.24 | 71.03 |
Table 29
| Two static mixers | Two separating tanks | Water wash column | |
| Cost of equipment (ten thousand yuan) | 1.0 | 3.5 | 18 |
| Add up to (ten thousand yuan) | 4.5 | 18 | |
As can be seen from the above Examples and Comparative Examples, set up the return wire of separation column C4 overhead fraction O7 to methyltertiarvbutyl ether reactor R1, can suppress the generation of the side reaction thing (dme) in the etherification reaction, improve the selectivity of methyl alcohol, promptly improve the utilization ratio of the methyl alcohol in the total system.Simultaneously, as can be seen from Table 29, be example as and if cracking associating preparing high-purity iso-butylene production equipment synthetic with 3.5 ten thousand tons of/year MTBE, replace water wash column can save about 13.5 ten thousand yuan of cost of equipment with static mixer and separating tank.
Claims (40)
1. the production technique of isoolefine and/or tert-alkyl ether, comprise that the hydrocarbon mixture and at least a alcohol that will contain a kind of isoolefine at least sends into etherification reaction zone (R1), the product that will contain tert-alkyl ether from least a portion that etherification reaction zone obtains is sent into fractionation zone (C1), to send into ether cracking zone (R2) from least a portion high purity tert-alkyl ether product that fractionation zone (C1) obtains, to send into from the product that contains isoolefine that ether cracking zone (R2) makes and take off heavy separation column (C3) or alcohol washing disengaging zone (L2), the at least a portion that will contain the cut of isoolefine from least a portion that separation column (C3) obtains or obtain from alcohol washing disengaging zone (L2) contains the organic phase of isoolefine and sends into alcohol washing disengaging zone (L2) or separation column (C3) respectively, to wash organic phase or the cut that at least a portion that disengaging zone (L2) or separation column (C3) obtain contains isoolefine from alcohol and send into separation column (C4), obtain the high purity isoolefine and mainly contain the overhead fraction of lower molecular weight ether light constituent, it is characterized in that at least a portion is circulated to etherification reaction zone (R1) from the overhead fraction that mainly contains lower molecular weight ether light constituent of separation column (C4).
2. the production technique of isoolefine according to claim 1 and/or tert-alkyl ether is characterized in that at least a portion is circulated to etherification reaction zone (R1) from the overhead fraction that contains unreacted hydrocarbon mixture, unreacting alcohol, a small amount of lower molecular weight ether light constituent of fractionation zone (C1).
3. the production technique of isoolefine according to claim 1 and/or tert-alkyl ether, it is characterized in that to send into earlier from the product that contains isoolefine that ether cracking zone (R2) makes and take off heavy separation column (C3), when sending into alcohol washing disengaging zone (L2) afterwards again, come the cut at the bottom of heavy separation column (C3) tower of autospasy to be circulated to etherification reaction zone (R1) at least a portion.
4. the production technique of isoolefine according to claim 1 and/or tert-alkyl ether, it is characterized in that sending into alcohol washing disengaging zone (L2) earlier when the product that contains isoolefine that makes from ether cracking zone (R2), send into again afterwards when taking off heavy separation column (C3), come cut at the bottom of heavy separation column (C3) tower of autospasy to be circulated to ether-splitting at least a portion and separate reaction zone (R2).
5. the production technique of isoolefine according to claim 1 and/or tert-alkyl ether, it is characterized in that at least a portion is sent into alcohol washing disengaging zone (L1) from the overhead fraction that fractionation zone (C1) contains unreacted hydrocarbon mixture, unreacting alcohol, a small amount of lower molecular weight ether light constituent, obtain water at the bottom of moisture, the pure tower and contain the organic phase of unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent.
6. the production technique of isoolefine according to claim 5 and/or tert-alkyl ether is characterized in that the organic phase that contains unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent that at least a portion is washed disengaging zone (L1) from alcohol is circulated to etherification reaction zone (R1).
7. the production technique of isoolefine according to claim 5 and/or tert-alkyl ether, it is characterized in that the organic phase that contains unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent that at least a portion is washed disengaging zone (L1) from alcohol being sent into separation column (C2), the overhead fraction that obtains containing the tower bottom distillate of unreacted hydrocarbon mixture and contain lower molecular weight ether.
8. the production technique of isoolefine according to claim 7 and/or tert-alkyl ether, it is characterized in that with at least a portion from mainly containing of separation column (C2) a small amount of lower molecular weight ether light constituent overhead fraction be circulated to etherification reaction zone (R1).
9. according to the production technique of each described isoolefine of claim 5-8 and/or tert-alkyl ether, it is characterized in that described alcohol washing disengaging zone (L1) selects at least one water wash column (T1) for use.
10. according to the production technique of each described isoolefine of claim 5-8 and/or tert-alkyl ether, it is characterized in that described alcohol washing disengaging zone (L1) selects at least one group of static mixer (Mn) and separating tank (Vn) for use.
11., it is characterized in that described alcohol washing disengaging zone (L2) selects at least one water wash column (T2) for use according to the production technique of each described isoolefine of claim 1-8 and/or tert-alkyl ether.
12., it is characterized in that described alcohol washing disengaging zone (L2) selects at least one group of static mixer (Mm) and separating tank (Vm) for use according to the production technique of each described isoolefine of claim 1-8 and/or tert-alkyl ether.
13. production technique according to each described isoolefine of claim 5-8 and/or tert-alkyl ether, it is characterized in that also comprising pure water separation column (C5), at least a portion is washed moisture, the pure water of disengaging zone (L1) from alcohol and/or moisture, pure water that at least a portion is washed disengaging zone (L2) from alcohol is sent into separation column (C5), with aqueous distillate and the rich pure cut that obtains poor alcohol.
14. the production technique of isoolefine according to claim 13 and/or tert-alkyl ether is characterized in that the pure cut of the described richness of at least a portion is circulated to etherification reaction zone (R1).
15. the production technique of isoolefine according to claim 13 and/or tert-alkyl ether is characterized in that the described aqueous distillate of at least a portion is circulated to alcohol washing disengaging zone (L1) and/or alcohol washing disengaging zone (L2).
16. the production technique of isoolefine according to claim 1 and/or tert-alkyl ether is characterized in that fresh water (W2) is introduced alcohol washing disengaging zone (L2).
17., it is characterized in that fresh water (W1) is introduced alcohol washing disengaging zone (L1) according to the production technique of each described isoolefine of claim 5-8 and/or tert-alkyl ether.
18. the production technique of isoolefine and/or tert-alkyl ether, comprise that the hydrocarbon mixture and at least a alcohol that will contain a kind of isoolefine at least sends into etherification reaction zone (R1), the product that will contain tert-alkyl ether from least a portion that etherification reaction zone obtains is sent into alcohol washing disengaging zone (L1), to wash the organic phase that contains tert-alkyl ether that disengaging zone (L1) obtains from alcohol and send into fractionation zone (C1), to send into ether cracking zone (R2) from least a portion high purity tert-alkyl ether product that fractionation zone (C1) obtains, the product that will contain isoolefine from least a portion that ether cracking zone (R2) makes is sent into and is taken off heavy separation column (C3) or alcohol washing disengaging zone (L2), the at least a portion that will contain the cut of isoolefine from least a portion that separation column (C3) obtains or obtain from alcohol washing disengaging zone (L2) contains the organic phase of isoolefine and sends into alcohol washing disengaging zone (L2) or separation column (C3) respectively, to wash organic phase or the cut that at least a portion that disengaging zone (L2) or separation column (C3) obtain contains isoolefine from alcohol and send into separation column (C4), obtain the high purity isoolefine and mainly contain the overhead fraction of lower molecular weight ether light constituent, it is characterized in that at least a portion is circulated to etherification reaction zone (R1) from the overhead fraction that mainly contains lower molecular weight ether light constituent of separation column (C4).
19. the production technique of isoolefine according to claim 18 and/or tert-alkyl ether is characterized in that at least a portion is circulated to etherification reaction zone (R1) from the overhead fraction that contains unreacted hydrocarbon mixture, unreacting alcohol, a small amount of lower molecular weight ether light constituent of fractionation zone (C1).
20. the production technique of isoolefine according to claim 18 and/or tert-alkyl ether, it is characterized in that to send into earlier from the product that contains isoolefine that ether cracking zone (R2) makes and take off heavy separation column (C3), when sending into alcohol washing disengaging zone (L2) afterwards again, come the cut at the bottom of heavy separation column (C3) tower of autospasy to be circulated to etherification reaction zone (R1) at least a portion.
21. the production technique of isoolefine according to claim 18 and/or tert-alkyl ether, it is characterized in that sending into alcohol washing disengaging zone (L2) earlier when the product that contains isoolefine that makes from ether cracking zone (R2), when taking off heavy separation column (C3) afterwards again, come cut at the bottom of heavy separation column (C3) tower of autospasy to be circulated to ether-splitting at least a portion and separate reaction zone (R2).
22. the production technique of isoolefine according to claim 18 and/or tert-alkyl ether, it is characterized in that at least a portion being sent into separation column (C2) from the overhead fraction that contains unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent of fractionation zone (C1), the overhead fraction that obtains containing the tower bottom distillate of unreacted hydrocarbon mixture and contain lower molecular weight ether.
23. the production technique of isoolefine according to claim 22 and/or tert-alkyl ether, it is characterized in that with at least a portion from mainly containing of separation column (C2) a small amount of lower molecular weight ether light constituent overhead fraction be circulated to etherification reaction zone (R1).
24., it is characterized in that described alcohol washing disengaging zone (L1) selects at least one water wash column (T1) for use according to the production technique of each described isoolefine of claim 18-23 and/or tert-alkyl ether.
25., it is characterized in that described alcohol washing disengaging zone (L1) selects at least one group of static mixer (Mn) and separating tank (Vn) for use according to the production technique of each described isoolefine of claim 18-23 and/or tert-alkyl ether.
26., it is characterized in that described alcohol washing disengaging zone (L2) selects at least one water wash column (T2) for use according to the production technique of claim 18-2 3 each described isoolefine and/or tert-alkyl ether.
27., it is characterized in that described alcohol washing disengaging zone (L2) selects at least one group of static mixer (Mm) and separating tank (Vm) for use according to the production technique of each described isoolefine of claim 18-23 and/or tert-alkyl ether.
28. production technique according to each described isoolefine of claim 18-23 and/or tert-alkyl ether, it is characterized in that also comprising pure water separation column (C5), at least a portion is washed moisture, the pure water of disengaging zone (L1) from alcohol and/or moisture, pure water that at least a portion is washed disengaging zone (L2) from alcohol is sent into separation column (C5), with aqueous distillate and the rich pure cut that obtains poor alcohol.
29. the production technique of isoolefine according to claim 28 and/or tert-alkyl ether is characterized in that the pure cut of the described richness of at least a portion is circulated to etherification reaction zone (R1).
30. the production technique of isoolefine according to claim 28 and/or tert-alkyl ether, it is characterized in that with the described aqueous distillate of at least a portion be circulated to alcohol washing disengaging zone (L1) and/or alcohol washing disengaging zone (L2).
31. the production technique of isoolefine according to claim 18 and/or tert-alkyl ether is characterized in that fresh water (W1) is introduced alcohol washing disengaging zone (L1) and/or fresh water (W2) is introduced alcohol washing disengaging zone (L2).
32. the production technique of isoolefine and/or tert-alkyl ether, comprise that the hydrocarbon mixture and at least a alcohol that will contain a kind of isoolefine at least sends into etherification reaction zone (R1), the product that will contain tert-alkyl ether from least a portion that etherification reaction zone obtains is sent into fractionation zone (C1) or alcohol washing disengaging zone (L1), the at least a portion that will obtain from fractionation zone (C1) or alcohol washing disengaging zone (L1) contains the unreacted hydrocarbon mixture, the cut of a small amount of lower molecular weight ether light constituent or organic phase are sent into alcohol washing disengaging zone (L1) or fractionation zone (C1), to wash at least a portion that disengaging zone (L1) or fractionation zone (C1) obtain from alcohol and contain the unreacted hydrocarbon mixture, the organic phase or the cut of a small amount of lower molecular weight ether light constituent are sent into separation column (C2), the overhead fraction that obtains containing the tower bottom distillate of unreacted hydrocarbon mixture and mainly contain lower molecular weight ether light constituent is characterized in that at least a portion is circulated to etherification reaction zone (R1) from the overhead fraction that mainly contains lower molecular weight ether light constituent of separation column (C2).
33. the production technique of isoolefine according to claim 32 and/or tert-alkyl ether is characterized in that at least a portion is circulated to etherification reaction zone (R1) from the overhead fraction that contains unreacted hydrocarbon mixture, unreacting alcohol, a small amount of lower molecular weight ether light constituent of fractionation zone (C1).
34. the production technique of isoolefine according to claim 32 and/or tert-alkyl ether, the organic phase that contains unreacted hydrocarbon mixture, a small amount of lower molecular weight ether light constituent that its feature is washed disengaging zone (L1) with at least a portion from alcohol is circulated to etherification reaction zone (R1).
35., it is characterized in that described alcohol washing disengaging zone (L1) selects at least one water wash column (T1) for use according to the production technique of each described isoolefine of claim 32-34 and/or tert-alkyl ether.
36., it is characterized in that described alcohol washing disengaging zone (L1) selects at least one group of static mixer (Mn) and separating tank (Vn) for use according to the production technique of each described isoolefine of claim 32-34 and/or tert-alkyl ether.
37. production technique according to each described isoolefine of claim 32-34 and/or tert-alkyl ether, it is characterized in that also comprising pure water separation column (C5), moisture, the pure water that at least a portion is washed disengaging zone (L1) from alcohol is sent into separation column (C5), with aqueous distillate and the rich pure cut that obtains poor alcohol.
38., it is characterized in that the pure cut of the described richness of at least a portion is circulated to etherification reaction zone (R1) according to the production technique of described isoolefine of claim 37 and/or tert-alkyl ether.
39., it is characterized in that the described aqueous distillate of at least a portion is circulated to alcohol washing disengaging zone (L1) according to the production technique of described isoolefine of claim 37 and/or tert-alkyl ether.
40., it is characterized in that fresh water (W1) is introduced alcohol washing disengaging zone (L1) according to the production technique of each described isoolefine of claim 32-34 and/or tert-alkyl ether.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001340905A CN1159272C (en) | 2000-12-13 | 2000-12-13 | Productive process for isoalkene and/or tertiary alkyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001340905A CN1159272C (en) | 2000-12-13 | 2000-12-13 | Productive process for isoalkene and/or tertiary alkyl ether |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1358698A CN1358698A (en) | 2002-07-17 |
| CN1159272C true CN1159272C (en) | 2004-07-28 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB001340905A Expired - Lifetime CN1159272C (en) | 2000-12-13 | 2000-12-13 | Productive process for isoalkene and/or tertiary alkyl ether |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102009027404A1 (en) * | 2009-07-01 | 2011-01-05 | Evonik Oxeno Gmbh | Preparation of isobutene by cleavage of MTBE |
| CN102070391B (en) * | 2011-01-12 | 2016-01-20 | 王伟跃 | The method of comprehensive utilization mixed c 4 preparing isobutene |
| CN103172487B (en) * | 2011-12-23 | 2015-05-13 | 中国石油化工股份有限公司 | Production process of high-purity isoolefine (tert-olefin) |
| CN103172483B (en) * | 2011-12-23 | 2015-05-13 | 中国石油化工股份有限公司 | Production process of high-purity isoolefine (tert-olefin) |
| ITMI20121673A1 (en) * | 2012-10-05 | 2014-04-06 | Saipem Spa | PROCEDURE FOR THE PRODUCTION OF ISOBUTENE WITH HIGH PURITY THROUGH THE CRACKING OF MTBE OR ETBE AND INTEGRATED PROCEDURE FOR THE PRODUCTION OF ITS ETHER |
| CN104892369B (en) * | 2015-05-22 | 2017-06-20 | 西安元创化工科技股份有限公司 | A kind of production technology of high-purity ethyl tert-butyl ether (ETBE) |
| CN106045810B (en) * | 2016-07-05 | 2018-10-19 | 中石化上海工程有限公司 | isobutene production method |
| KR102086563B1 (en) * | 2017-01-06 | 2020-03-09 | 주식회사 엘지화학 | Method for producing methyl tert-butylether |
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2000
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| CN1358698A (en) | 2002-07-17 |
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