CN204607890U - A kind of device utilizing new catalytic rectifying structured packing to produce MTBE - Google Patents
A kind of device utilizing new catalytic rectifying structured packing to produce MTBE Download PDFInfo
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- CN204607890U CN204607890U CN201520278138.8U CN201520278138U CN204607890U CN 204607890 U CN204607890 U CN 204607890U CN 201520278138 U CN201520278138 U CN 201520278138U CN 204607890 U CN204607890 U CN 204607890U
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- 230000003197 catalytic effect Effects 0.000 title claims abstract description 68
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 238000012856 packing Methods 0.000 title claims abstract description 21
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 311
- 238000003808 methanol extraction Methods 0.000 claims abstract description 54
- 238000004821 distillation Methods 0.000 claims abstract description 47
- 238000011084 recovery Methods 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 21
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000006266 etherification reaction Methods 0.000 claims abstract description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- 239000007864 aqueous solution Substances 0.000 abstract description 5
- 230000009466 transformation Effects 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract description 2
- 238000000605 extraction Methods 0.000 description 34
- 239000000203 mixture Substances 0.000 description 19
- 239000000047 product Substances 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 239000002994 raw material Substances 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 9
- 238000010992 reflux Methods 0.000 description 6
- 239000004615 ingredient Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 150000001336 alkenes Chemical class 0.000 description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 4
- 239000013589 supplement Substances 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000013461 intermediate chemical Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 230000001839 systemic circulation Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of device utilizing new catalytic rectifying structured packing to produce MTBE, comprises pre-reactor, catalytic rectifying column, methanol extraction tower, methanol distillation column and recovery of heat mixing tank, MTBE is generated at pre-reactor generation etherification reaction containing the C4 of iso-butylene and methanol mixed, reacted material by pump delivery to catalytic rectifying column, new methyl alcohol is supplemented again in tower, there is etherification reaction further in iso-butylene and methyl alcohol, total conversion rate reaches more than 99.5%, through refinery distillation, MTBE product distillates at the bottom of tower, unreacted C4 and methyl alcohol etc. distillate from tower top, enter methanol extraction tower, water enters from methanol extraction tower top, methanol aqueous solution at the bottom of tower out, enter methanol distillation column, methyl alcohol ejects from methanol distillation column and returns pre-reactor, water out at the bottom of tower returns to methanol extraction tower top with the new water supplemented through recovery of heat mixing tank, recycle.The transformation efficiency that the utility model structure is simple, effective, improve iso-butylene, improves the product purity of MTBE.
Description
Technical field
The utility model relates to a kind of device utilizing new catalytic rectifying structured packing to produce MTBE, belongs to technical field of petrochemical industry.
Background technology
Methyl tertiary butyl ether (MTBE) has the feature that octane value is high, steam forces down that is in harmonious proportion, and be the carrier of oxygen, there is lower air active, significantly can reduce the discharge of CO and unburn hydro carbons, desirable processed oil blend component, with iso-butylene in carbon four and methyl alcohol for raw material production MTBE is present industrial main method.
The main method utilizing iso-butylene in carbon four (C4) mixture to produce MTBE is at present: the C 4 mixture containing iso-butylene fully mixes through pre-reactor with methyl alcohol after weight is separated, mixing raw material enters and is equipped with in the cleaner of cation exchange resin catalyst after feed heater preheating, remove alkali wherein and alkalimetal ion, then after feed cooler cooling, enter reactor and carry out etherification reaction, eventually pass catalytic fractionator limit coronite to be separated, obtain the process mode of product MTBE.
A kind of MTBE of utility model patent produces in purifying plant (CN201320251237) to disclose and first carbon four raw material is carried out decarburization five operation, then with methanol feedstock static mixing, enter follow-up MTBE catalyst etherifying synthesis, the wherein rank of not mentioned MTBE product; Utility model patent a kind of by carbon four with the method (CN200810143656) of methanol production high purity MTBE, utilize and increase carbon five sepn process, after catalyst etherifying unit, the operation of decarburization five separation and purification is carried out to the thick product of MTBE, make product purity be stabilized in more than 99.0%.No matter both are carry out decarburization five operation from the front and back of MTBE building-up process, all correspondingly increase facility investment and operation easier etc.And iso-butylene and methyl alcohol generation building-up reactions obtain methyl tertiary butyl ether, this reaction process is reversible reaction, the purity of reaction product is subject to the restriction of many factors in reversible reaction process, therefore, in actual production process, designing a set of production process production unit that is reasonable, that can improve product purity becomes the technical barrier that those skilled in the art need solution badly.
Utility model content
Utility model object: the purpose of this utility model is a kind of device utilizing new catalytic rectifying structured packing to produce MTBE, improve the transformation efficiency of iso-butylene, improve the product purity of MTBE, there is higher product utilization be worth, be not only as oil dope, improve octane value, and can be used as chemical industry monomer product.
Technical scheme: a kind of device utilizing new catalytic rectifying structured packing to produce MTBE described in the utility model, comprises pre-reactor, catalytic rectifying column, methanol extraction tower, methanol distillation column and recovery of heat mixing tank,
Described pre-reactor top is provided with pre-reactor opening for feed, and bottom is provided with pre-reactor discharge port;
Described catalytic rectifying column tower top is provided with catalytic rectifying column tower top discharge port, and top is provided with catalytic rectifying column methanol feeding mouth and catalytic rectifying column opening for feed, is provided with outlet for product after etherificate at the bottom of tower;
Described methanol extraction tower top is provided with supplementary feed opening for feed, and bottom is provided with methanol extraction tower opening for feed, and tower top is provided with methanol extraction column overhead discharge port, is provided with discharge port at the bottom of methanol extraction tower tower at the bottom of tower;
Be provided with methanol distillation column opening for feed in the middle part of described methanol distillation column, tower top is provided with Methanol Recovery column overhead discharge port, is provided with discharge port at the bottom of methanol distillation column tower at the bottom of tower;
The pre-reactor discharge port of described pre-reactor connects the catalytic rectifying column opening for feed of catalytic rectifying column, the catalytic rectifying column tower top discharge port of described catalytic rectifying column connects the methanol extraction tower opening for feed of methanol extraction tower, and at the bottom of the methanol extraction tower tower of described methanol extraction tower, discharge port connects the methanol distillation column opening for feed of methanol distillation column;
The pre-reactor opening for feed on described pre-reactor top is connected with pre-reactor methanol feed line and carbon four feeding line containing iso-butylene, the Methanol Recovery column overhead discharge port of described methanol distillation column is connected with pre-reactor methanol feed line;
The supplementary feed opening for feed of described methanol extraction tower is connected with waterworks, described waterworks is made up of recovery of heat mixing tank and the water pipe being connected to its two ends, discharge port at the bottom of the methanol distillation column tower of described methanol distillation column is connected with the import of recovery of heat mixing tank thermal source, and supplementary feed is sent in methanol extraction tower by water pipe after the direct heat exchange of recovery of heat mixing tank.
Further: the rectifying section of described catalytic rectifying column, stripping section and etherification reaction section all adopt window diversion type structured packing.
Adopt the device of above-mentioned production MTBE to carry out the method for MTBE production, comprise the steps:
1.1, the C4 raw material and methyl alcohol that contain iso-butylene are entered pre-reactor from pre-reactor opening for feed, carry out preliminary etherification reaction containing the C4 raw material of iso-butylene and methyl alcohol and generate MTBE, the transformation efficiency of active olefin is 90-92%, and reacted mixture is by the extraction of pre-reactor discharge port;
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column opening for feed, catalytic rectifying column methanol feeding mouth respectively, there is etherification reaction further and generate MTBE in iso-butylene and methyl alcohol, after twice etherification reaction, active olefin total conversion rate reaches more than 99.5%, through refinery distillation, MTBE product distillates from outlet for product after etherificate at the bottom of tower, and remaining ingredient mixture distillates from catalytic rectifying column tower top discharge port;
1.3, the remaining ingredient mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower through recovery of heat mixing tank by supplementary feed opening for feed, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, and remaining ingredient is by the extraction of methanol extraction column overhead discharge port;
1.4, the methanol aqueous solution of step 1.3 extraction enters methanol distillation column by methanol distillation column mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of Methanol Recovery column overhead discharge port, and water is from discharge port extraction at the bottom of methanol distillation column tower;
1.5, the methyl alcohol of extraction in step 1.4 enters pre-reactor by pre-reactor methanol feed line, recycles; The water of extraction enters methanol extraction tower and recycles after recovery of heat mixing tank with the new water direct heat-exchange supplemented.
Improve technique scheme further, the working temperature of described pre-reactor is 50-80 DEG C, and pre-reactor working pressure is 0.5-0.8MPa.
The theoretical plate number of described catalytic rectifying column is 30-70 block, and working pressure is 0.4-0.7Mpa.
The working pressure of described methanol extraction tower and methanol distillation column is 0.15-0.5Mpa.
Compared with prior art, its beneficial effect is the utility model:
(1) structural shape of catalytic rectifying column adopts window diversion type structured packing catalyzer, effectively increases gas-liquid mass transfer area, improves gas-liquid mass transfer speed, improve mass-transfer efficiency further.
(2) whole technique and device, achieves the cyclically utilizing of two intermediate chemical: the systemic circulation of extraction agent-water, and in process, loss is less; Methyl alcohol after extraction is through methanol distillation column Posterior circle reuse feed circuit, and raw material material consumption reduces greatly.
(3) in technological process, achieve the recycling of heat energy, improve the resource utilization of system process.
(4) the utility model structure is simple, effective, transformation efficiency is high, is an energy-conserving and environment-protective technology, meets industry development relevant policies.
Accompanying drawing explanation
Fig. 1 is the apparatus structure schematic diagram utilizing new catalytic rectifying structured packing to produce MTBE a kind of described in embodiment 1.
Fig. 2 is that catalytic rectifying column packing layer assembly A and assembly B stacks and the vertical view of curling placement.
Fig. 3 to be catalytic rectifying column packing layer assembly A with assembly B be alternately arranged vertical vertical view placed.
Fig. 4 is the center section schematic diagram of Fig. 3.
In figure: 1-pre-reactor, 1-catalytic rectifying column, 3-methanol extraction tower, 4-methanol distillation column, 7-recovery of heat mixing tank, 5-assembly A, 6-assembly B, a-methanol feeding, b-is containing iso-butylene C4 charging, c-supplements methanol feeding, and d-remains C4 component, the charging of e-supplementary feed, f-MTBE product.
Embodiment
Below in conjunction with accompanying drawing, technical solutions of the utility model are described in detail, but protection domain of the present utility model is not limited to described embodiment.
Embodiment 1: a kind of device utilizing new catalytic rectifying structured packing to produce MTBE, comprises pre-reactor 1, catalytic rectifying column 2, methanol extraction tower 3, methanol distillation column 4 and recovery of heat mixing tank 7.
Described pre-reactor 1 top is provided with pre-reactor opening for feed, and bottom is provided with pre-reactor discharge port;
Described catalytic rectifying column 2 tower top is provided with catalytic rectifying column tower top discharge port, and top is provided with catalytic rectifying column methanol feeding mouth and catalytic rectifying column opening for feed, is provided with outlet for product after etherificate at the bottom of tower;
The rectifying section of described catalytic rectifying column, stripping section and etherification reaction section all adopt window diversion type structured packing, assembly A and the assembly B of two kinds of different structures is comprised in every layer of packing layer, assembly A be window diversion packing sheet external parcel silk screen, in fill out ion exchange resin and fill catalyzer, assembly B is structured packing sheet, assembly A and assembly B stacks and curling, then fix with banding sheet, form catalytic rectification packing, as shown in Figure 2.
As replacement, assembly A and assembly B also can be alternately arranged vertical placement in every layer of packing layer, as shown in Figures 3 and 4.
Described methanol extraction tower 3 top is provided with supplementary feed opening for feed, and bottom is provided with methanol extraction tower opening for feed, and tower top is provided with methanol extraction column overhead discharge port, is provided with discharge port at the bottom of methanol extraction tower tower at the bottom of tower;
Be provided with methanol distillation column opening for feed in the middle part of described methanol distillation column 4, tower top is provided with Methanol Recovery column overhead discharge port, is provided with discharge port at the bottom of methanol distillation column tower at the bottom of tower;
The pre-reactor discharge port of described pre-reactor 1 connects the catalytic rectifying column opening for feed of catalytic rectifying column 2, the catalytic rectifying column tower top discharge port of described catalytic rectifying column 2 connects the methanol extraction tower opening for feed of methanol extraction tower 3, and at the bottom of the methanol extraction tower tower of described methanol extraction tower 3, discharge port connects the methanol distillation column opening for feed of methanol distillation column 4;
The pre-reactor opening for feed on described pre-reactor 1 top is connected with pre-reactor methanol feed line and carbon four feeding line containing iso-butylene, the Methanol Recovery column overhead discharge port of described methanol distillation column 4 is connected with pre-reactor methanol feed line;
The supplementary feed opening for feed of described methanol extraction tower 3 is connected with waterworks, described waterworks is made up of recovery of heat mixing tank 7 and the water pipe being connected to its two ends, discharge port at the bottom of the methanol distillation column tower of described methanol distillation column 4 is connected with the import of recovery of heat mixing tank 7 thermal source, and supplementary feed is sent in methanol extraction tower 3 by water pipe after recovery of heat mixing tank 7 direct heat exchange.
Adopt the device of above-mentioned production MTBE to carry out the method for MTBE production, comprise the steps:
1.1, the C4 raw material and methyl alcohol that contain iso-butylene are entered pre-reactor from pre-reactor opening for feed, carry out preliminary etherification reaction containing the C4 raw material of iso-butylene and methyl alcohol and generate MTBE, the transformation efficiency of active olefin is 90-92%, and reacted mixture is by the extraction of pre-reactor discharge port.
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column opening for feed, catalytic rectifying column methanol feeding mouth respectively, there is etherification reaction further and generate MTBE in iso-butylene and methyl alcohol, after twice etherification reaction, active olefin total conversion rate reaches more than 99.5%, through refinery distillation, MTBE product distillates from outlet for product after etherificate at the bottom of tower, and remaining ingredient mixture distillates from catalytic rectifying column tower top discharge port.
1.3, the remaining ingredient mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower through recovery of heat mixing tank by supplementary feed opening for feed, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, residue C4 component, by the extraction of methanol extraction column overhead discharge port, carries out follow-up comprehensive utilization.
1.4, the methanol aqueous solution of step 1.3 extraction enters methanol distillation column by methanol distillation column mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of Methanol Recovery column overhead discharge port, and water is from discharge port extraction at the bottom of methanol distillation column tower;
1.5, the methyl alcohol of extraction in step 1.4 enters pre-reactor by pre-reactor methanol feed line, recycles; The water of extraction enters methanol extraction tower and recycles after recovery of heat mixing tank with the new water direct heat-exchange supplemented.
Wherein: the feed rate that C4 raw material enters pre-reactor is 5150kg/h, the feed rate that methyl alcohol enters pre-reactor is 928.883kg/h, and the feed rate that supplementary methyl alcohol enters catalytic rectifying column is 38kg/h.Pre-reactor working temperature is 70 DEG C, and working pressure is 0.7Mpa; Catalytic rectifying column number of theoretical plate is 50, working pressure 0.57Mpa, and mixture opening for feed is positioned at the 22nd piece of theoretical stage place, and supplement methanol feeding mouth and be positioned at the 10th theoretical stage place, catalytic rectifying column reflux ratio is 1; Methanol extraction tower stage number is 10, and working pressure is 0.37Mpa, and it is 200kg/h that supplementary feed enters flow; Methanol distillation column stage number is 25, and working pressure is 0.2Mpa, and reflux ratio is 6.
Table 1: the methyl alcohol liquid phase flow rate of extraction phase and recycle after extraction at the bottom of pre-reactor feed inlet and outlet, catalytic rectifying column overhead extraction and tower in embodiment 1, extraction and composition
Embodiment 2: adopt apparatus and method of producing MTBE identical with embodiment 1.
Difference is: the feed rate that C4 raw material enters pre-reactor is 2000kg/h, and the feed rate that methyl alcohol enters pre-reactor is 300kg/h, and the feed rate that supplementary methyl alcohol enters catalytic rectifying column is 17kg/h.Pre-reactor working temperature is 60 DEG C, and working pressure is 0.6Mpa; Catalytic rectifying column number of theoretical plate is 50, working pressure 0.5Mpa, and mixture opening for feed is positioned at the 22nd piece of theoretical stage place, and supplement methanol feeding mouth and be positioned at the 10th theoretical stage place, catalytic rectifying column reflux ratio is 1.5; Methanol extraction tower stage number is 10, and working pressure is 0.25Mpa, and supplementary feed feed rate is 70kg/h; Methanol distillation column stage number is 20, and working pressure is 0.25Mpa, and reflux ratio is 5.
Table 2: the methyl alcohol liquid phase flow rate of extraction phase and recycle after extraction at the bottom of pre-reactor feed inlet and outlet, catalytic rectifying column overhead extraction and tower in embodiment 2, extraction and composition
Embodiment 3: adopt apparatus and method of producing MTBE identical with embodiment 1.
Difference is: the feed rate that C4 raw material enters pre-reactor is 8000kg/h, and the feed rate that methyl alcohol enters pre-reactor is 1300kg/h, and the feed rate that supplementary methyl alcohol enters catalytic rectifying column is 160kg/h.Pre-reactor working temperature is 65 DEG C, and working pressure is 0.6Mpa; Catalytic rectifying column number of theoretical plate is 60, working pressure 0.6Mpa, and mixture opening for feed is positioned at the 30th piece of theoretical stage place, and supplement methanol feeding mouth and be positioned at the 8th theoretical stage place, catalytic rectifying column reflux ratio is 2; Methanol extraction tower stage number is 10, and working pressure is 0.35Mpa, and supplementary feed feed rate is 360kg/h; Methanol distillation column stage number is 35, and working pressure is 0.15Mpa, and reflux ratio is 4.5.
Table 3: the methyl alcohol liquid phase flow rate of extraction phase and recycle after extraction at the bottom of pre-reactor feed inlet and outlet, catalytic rectifying column overhead extraction and tower in embodiment 3, extraction and composition
As mentioned above, although represented with reference to specific preferred embodiment and described the utility model, it shall not be construed as the restriction to the utility model self.Under the spirit and scope prerequisite of the present utility model not departing from claims definition, various change can be made in the form and details to it.
Claims (2)
1. utilize new catalytic rectifying structured packing to produce a device of MTBE, it is characterized in that: comprise pre-reactor, catalytic rectifying column, methanol extraction tower, methanol distillation column and recovery of heat mixing tank,
Described pre-reactor top is provided with pre-reactor opening for feed, and bottom is provided with pre-reactor discharge port;
Described catalytic rectifying column tower top is provided with catalytic rectifying column tower top discharge port, and top is provided with catalytic rectifying column methanol feeding mouth and catalytic rectifying column opening for feed, is provided with outlet for product after etherificate at the bottom of tower;
Described methanol extraction tower top is provided with supplementary feed opening for feed, and bottom is provided with methanol extraction tower opening for feed, and tower top is provided with methanol extraction column overhead discharge port, is provided with discharge port at the bottom of methanol extraction tower tower at the bottom of tower;
Be provided with methanol distillation column opening for feed in the middle part of described methanol distillation column, tower top is provided with Methanol Recovery column overhead discharge port, is provided with discharge port at the bottom of methanol distillation column tower at the bottom of tower;
The pre-reactor discharge port of described pre-reactor connects the catalytic rectifying column opening for feed of catalytic rectifying column, the catalytic rectifying column tower top discharge port of described catalytic rectifying column connects the methanol extraction tower opening for feed of methanol extraction tower, and at the bottom of the methanol extraction tower tower of described methanol extraction tower, discharge port connects the methanol distillation column opening for feed of methanol distillation column;
The pre-reactor opening for feed on described pre-reactor top is connected with pre-reactor methanol feed line and carbon four feeding line containing iso-butylene, the Methanol Recovery column overhead discharge port of described methanol distillation column is connected with pre-reactor methanol feed line;
The supplementary feed opening for feed of described methanol extraction tower is connected with waterworks, described waterworks is made up of recovery of heat mixing tank and the water pipe being connected to its two ends, discharge port at the bottom of the methanol distillation column tower of described methanol distillation column is connected with the import of recovery of heat mixing tank thermal source, and supplementary feed is sent in methanol extraction tower after the direct heat exchange of recovery of heat mixing tank.
2. according to claim 1ly a kind ofly utilize new catalytic rectifying structured packing to produce the device of MTBE, it is characterized in that: the rectifying section of described catalytic rectifying column, stripping section and etherification reaction section all adopt window diversion type structured packing.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104829435A (en) * | 2015-04-30 | 2015-08-12 | 中建安装工程有限公司 | Apparatus for producing MTBE by using novel catalytic distillation structured packing, and method thereof |
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Address after: 210000 Yaojia Road, Qixia District, Nanjing, Jiangsu Province Patentee after: CHINA CONSTRUCTION INDUSTRIAL & ENERGY ENGINEERING GROUP Co.,Ltd. Address before: 210000 Yaojia Road, Qixia District, Nanjing, Jiangsu Province Patentee before: China Construction Installation Engineering Co.,Ltd. |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150902 |