CN108558603B - Three-tower three-effect crude methanol refining process method - Google Patents
Three-tower three-effect crude methanol refining process method Download PDFInfo
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Abstract
The invention provides a three-tower triple-effect crude methanol refining process method, which enables the gas phase heat of refined methanol extracted from the top of a pressurized rectifying tower to firstly meet the reboiling load of the bottom of an atmospheric rectifying tower, and the residual gas phase heat of the refined methanol provides partial heat for the reboiling of the bottom of a pre-rectifying tower. The heat distribution of the two parts can ensure that the heat of the gas-phase material at the top of the pressurized rectifying tower is reasonably distributed and utilized to the maximum extent, and the energy consumption of the system is effectively reduced.
Description
Technical Field
The invention belongs to the technical field of chemical material purification process methods and equipment, and particularly relates to a crude methanol refining method and a crude methanol refining system.
Background
Methanol is an important basic organic chemical raw material and novel energy fuel, almost all industrially synthesized methanol adopts a carbon monoxide pressurized catalytic hydrogenation method, the process comprises the working procedures of gas making, synthesis and purification, methanol synthesis, crude methanol rectification and the like, and the methanol rectification mainly aims at removing volatile components such as dimethyl ether, ethanol which is difficult to volatilize, higher alcohol and water to produce refined methanol which meets the product requirements. With the vigorous development of the coal chemical industry, the scale of the methanol rectification device is larger and larger, how to reduce the energy consumption of a single ton of refined methanol of the methanol refining device becomes the key for the survival of enterprises and the improvement of competitiveness, and the research workers take the energy consumption as a research object to carry out deep research.
The currently widely adopted three-tower methanol rectification (concurrent double-effect rectification) process is that crude methanol is rectified and separated sequentially through a pre-rectification tower, a pressurized rectification tower and an atmospheric rectification tower, and methanol products are respectively obtained through the discharge at the top of the pressurized tower and the discharge at the top of the atmospheric tower. The separation sequence is that a pre-rectifying tower removes light components in the crude methanol, the prognostic crude methanol at the tower bottom enters a pressurized rectifying tower, the condensation latent heat of methanol steam at the top of the pressurized tower is used as a reboiling heat source of an atmospheric tower to realize forward flow double-effect rectification, the fusel is extracted from the side line of the atmospheric tower, and the waste water is discharged from the bottom of the atmospheric tower. The method is a common crude methanol refining process, the energy consumption of the methanol refining process is about 3223.7 MJ/ton of methanol product, the production energy consumption is higher, and the total energy consumption is also obviously increased along with the expansion of the methanol refining scale.
In order to reduce the energy consumption of methanol distillation, the prior art has various attempted solutions, such as adding to five-tower distillation or adopting heat pump technology. However, five-tower rectification directly causes other problems such as site and tower investment, consumption of condensed water and the like, and heat pump rectification also has the problems of equipment investment and power consumption.
Disclosure of Invention
The invention aims to provide a three-tower triple-effect crude methanol refining process method, which can reduce the energy consumption of a system and reduce the equipment investment.
The three-tower three-effect crude methanol refining process method ensures that the gas phase heat of the refined methanol extracted from the top of the pressurized rectifying tower firstly meets the reboiling load of the bottom of the atmospheric rectifying tower, and the residual gas phase heat of the refined methanol provides partial heat for the reboiling of the bottom of the pre-rectifying tower. The heat distribution of the two parts can ensure that the heat of the gas-phase material at the top of the pressurized rectifying tower is reasonably distributed and utilized to the maximum extent, and the energy consumption of the system is effectively reduced.
Specifically, after crude methanol enters a pre-rectifying tower, light components and a small amount of gaseous methanol are extracted from the top of the pre-rectifying tower, and an aqueous methanol solution A is extracted from the bottom of the pre-rectifying tower and enters a pressurized rectifying tower; the refined methanol gas phase material extracted from the top of the pressurized rectifying tower is divided into two parts: one is sent to the bottom of the atmospheric distillation tower and provides heat required by reboiling for the atmospheric distillation tower, and the other is sent to the bottom of the pre-rectification tower and provides partial heat required by reboiling for the pre-rectification tower; after heat exchange, the two strands of refined methanol gas phase materials become refined methanol condensate respectively and are combined; the combined refined methanol condensate is divided into at least two parts: one as reflux liquid and reflux into the pressurized rectifying tower and the other as product; the aqueous methanol solution B extracted from the bottom of the pressurized rectifying tower enters a normal pressure rectifying tower; the refined methanol gas phase material extracted from the top of the atmospheric distillation tower is divided into two parts: one strand is taken as a product, and the other strand forms reflux liquid and flows back into the normal pressure rectifying tower; and wastewater materials are extracted from the bottom of the atmospheric distillation tower.
The number of the plates of the pre-rectifying tower is 50-60 layers, the temperature extracted from the top of the tower is 60-65 ℃, the pressure is 110-165 kPa, the reflux ratio is 5.0-9.5, the temperature extracted from the bottom of the tower is 79-83 ℃, and the pressure is 160-165 kPa; the tower plate number of the pressurized rectifying tower is 70-90 layers, the temperature extracted from the tower top is 120-130 ℃, the pressure is 700-750kPa, the reflux ratio is 2.0-4.2, the temperature extracted from the tower bottom is 125-135 ℃, and the pressure is 750-800 kPa; the tower plate number of the normal pressure rectifying tower is 80-100 layers, the temperature of the tower top is 70-80 ℃, the pressure is 140kPa, the reflux ratio is 1.5-3.5, the temperature of the tower bottom is 110-120 ℃, and the pressure is 167-190 kPa.
The optimized control of the process conditions further optimizes and reduces the energy consumption of the system under the condition of ensuring the purity of the refined methanol.
Wherein the feed composition of the crude methanol is: the methanol content is 85-95w%, the light component impurity is 1.5-2.5w%, and the heavy component impurity is 2.5-13.5 w%; the methanol content in the gas phase material extracted from the top of the pre-rectifying tower is 60-65w%, and the methanol content in the aqueous methanol solution A extracted from the bottom of the pre-rectifying tower is 70-85 w%; the content of methanol in the aqueous methanol solution A extracted from the bottom of the pressurized rectifying tower is 70-75 w%. The optimized control of the feeding and discharging components ensures that the purification efficiency can be optimized while the purity of the refined methanol is ensured and the energy consumption is reduced.
And gas-liquid separation is carried out on the gas-phase material extracted from the top of the pre-rectifying tower after primary condensation and secondary condensation respectively, the separated liquid serving as reflux liquid flows back to the pre-rectifying tower, and the separated gas and the noncondensable gas after secondary condensation are combined and sent to a subsequent treatment system. The secondary condensation is adopted to improve the condensation recovery efficiency and reduce the loss rate of methanol.
Wherein, the bottom of the pre-rectifying tower is provided with at least two reboiling devices, preferably three reboiling devices, and one reboiling device is thermally coupled with one strand of the refined methanol gas-phase material extracted from the top of the pressurized rectifying tower. The reboiling device which is thermally coupled with the refined methanol gas-phase material is independently arranged, the investment cost is low, the transformation efficiency is high, the operation and the control are facilitated, the reliability of thermal coupling can be effectively improved, and the effective utilization rate of heat flow is improved.
And after the refined methanol gas-phase materials extracted from the top of the pressurized rectifying tower are subjected to heat exchange to become refined methanol condensate and are combined, the non-condensable gas in the refined methanol gas-phase materials is taken as a third stream and is combined with the gas-phase materials extracted from the top of the atmospheric rectifying tower in a gas form for extraction. On one hand, the non-condensable gas can be further recycled, and energy waste and influence on the operation stability of the system caused by re-entering the pressurized rectifying tower can be avoided.
Wherein, the refined methanol gas phase material extracted from the top of the atmospheric distillation tower is divided into two parts after condensation: one strand of the liquid is used as reflux liquid and flows back into a normal pressure rectifying tower; the other is further cooled and withdrawn as product.
Wherein fusel is also extracted from the middle lower part of the atmospheric distillation tower, the water content of the fusel is 50-80 w%, the extraction temperature is 95-101 ℃, and the pressure is 110-170 KPa. The design of the fusel extraction line is beneficial to reducing the load of the atmospheric distillation tower, improving the refining efficiency of methanol, further reducing the energy consumption, and the recovered fusel can be further treated to obtain resource recycling.
Compared with the prior art, the invention has the following advantages: the process method is easy to control and implement, small in equipment investment and strong in operability, can effectively reduce the unit energy consumption of methanol refining, does not need to occupy additional fields, and is easy to realize the rapid reconstruction of the existing engineering.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate an embodiment of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 is a process flow diagram of the present invention. Wherein the coarse blue line is a liquid phase process stream and the fine powder line is a gas phase process stream.
Detailed Description
For a better understanding of the present invention, reference is made to the following detailed description taken in conjunction with the accompanying drawings. The following examples illustrate details of the process for the purpose of describing the invention in detail and are not intended to unduly limit the invention.
As shown in fig. 1, crude methanol (feed R1) was preheated by a first preheater M4 into a pre-rectification column M1 at a feed temperature of 60 c, within which 52 high efficiency DVST trays were placed. Light components and a small part of methanol in a gaseous form in the crude methanol are extracted from the top of a pre-rectifying tower M1, the content of the methanol in gas-phase materials extracted from the top of the pre-rectifying tower is about 63%, the temperature extracted from the top of the pre-rectifying tower is 64.7 ℃, the pressure is 129KPa, the gas-phase materials extracted from the top of the pre-rectifying tower are subjected to secondary condensation through a first condenser M5 and a second condenser M6 respectively, the temperature of the materials is reduced to 40 ℃, non-condensable gas after the secondary condensation is sent to a subsequent torch system, condensate after the secondary condensation is sent to a gas-liquid separator M7 for further gas-liquid separation, separated liquid after the gas-liquid separation enters a 52 th layer of tower plate at the top of the pre-rectifying tower M1 through a first reflux tank M8 for reflux, the reflux ratio is 5.5, the temperature of the reflux liquid is 40 ℃, and the separated gas after the gas-liquid separation and the non-condensable gas after the secondary condensation are combined and sent to the subsequent torch system. The condensate in the first condenser M5 directly enters the first reflux tank M8, and the non-condensable gas phase in the first reflux tank M8 flows back to the second condenser M6 to be condensed.
At least two reboilers, in this case three reboilers, namely a reboiler M9, a reboiler M10 and a reboiler M11, are connected in parallel to the bottom of the pre-rectifying column M1. The reboiler M10 and reboiler M11 provide heat through external steam lines, respectively. One side of one reboiler M11 is provided with a buffer tank M12, gas phase materials extracted from the top of the pressurized rectifying tower M2 enter the buffer tank M12, then are thermally coupled (heat exchanged) with the reboiler M11 to be cooled to form condensate, and the condensate returns to a second reflux tank M16 of the pressurized rectifying tower M2.
Aqueous methanol solution A (material R2) is extracted from the bottom of the pre-rectifying tower M1, wherein the content of the methanol is about 83.6 percent, and the aqueous methanol solution A is extracted from the bottom of the pre-rectifying tower M3578At a temperature of 80.4 ℃ and a pressure of 1.6kg/cm2. The aqueous methanol solution A is preheated by a second preheater M13 and then enters the pressurized rectifying tower M2 above the middle-lower tray, and the feeding temperature is 125 ℃. The second preheater M13 provides heat through an external steam line. The pressurized rectifying column M2 was equipped with 85 high-efficiency DVST trays. The gas phase material extracted from the top of the tower is refined methanol, the content of the methanol is 99.991%, the temperature extracted from the top of the tower is 122.6 ℃, and the pressure is 7.0kg/cm2. The refined methanol gas phase material extracted from the tower top is divided into two parts: one strand (material R4) preferentially enters a reboiler M19 at the bottom of an atmospheric distillation tower M3 to provide heat required by the reboiler M19, so that an external heat source is not required to be introduced in the reboiling process at the bottom of the atmospheric distillation tower M3, and a refined methanol condensate condensed after heat exchange enters a second reflux tank M16 of a pressurized distillation tower M2; the other stream (material R5) enters a reboiler M11 at the bottom of the pre-rectifying tower M1 as described above to provide required heat for the reboiler M11, so that the total consumption of steam required by the reboiling process at the bottom of the pre-rectifying tower M1 is reduced, and the condensed refined methanol condensate after heat exchange also enters a second reflux tank M16. The refined methanol condensate in the second reflux tank M16 is also divided into two or three streams: one strand enters a tower plate at the top 85 th layer of a pressurized rectifying tower M2 for reflux, the reflux ratio is 2.2, and the reflux liquid temperature is 122.6 ℃; the second strand is cooled for the second time by a first cooler M17 and a second cooler M18 in sequence and then enters a product storage tank; the third strand is formed when the refined methanol condensate which flows back to the second reflux tank M16 contains certain non-condensable gas, and the third strand does not generate non-condensable gas under some working conditions, so that the third strand does not exist.
At least one reboiler, in this case two reboilers M14 and M15, are connected in parallel to the bottom of the pressurized rectifying column M2, and they supply heat through external steam lines.
The bottom of the pressurized rectifying tower M2 produces aqueous methanol solution B (material R3), wherein the content of methanol is about 70.3%, the temperature of the bottom produced is 132.7 ℃, and the pressure is 7.6kg/cm2. The aqueous methanol solution B enters a middle-lower tray of an atmospheric distillation tower M3Above, the feed temperature was 125 ℃. The atmospheric rectification column M3 is internally provided with 90 layers of high-efficiency DVST trays. The gas phase material extracted from the top of the tower is refined methanol (material R6), the methanol content is 99.994%, the temperature extracted from the top of the tower is 72.3 ℃, and the pressure is 1.4kg/cm2. And (3) the refined methanol gas-phase material extracted from the tower top enters a third reflux tank M21 through a third condenser M20 to be condensed and cooled, and the condensed and cooled material is divided into two parts: one strand enters a 90 th layer of tower plate at the top of the atmospheric distillation tower M3 for reflux, the reflux ratio is 1.7, and the temperature of reflux liquid is 72.3 ℃; the other strand enters the product storage tank after being cooled by a third cooler M22.
The wastewater material (material R7) is extracted from the bottom of the atmospheric distillation tower M3, wherein the water content is 99.8%, the temperature extracted from the bottom of the tower is 114.1 ℃, and the pressure is 1.7kg/cm2. After being cooled by the fourth cooler M25, the waste is sent to a subsequent waste treatment system for treatment.
The middle lower part of the atmospheric distillation tower M3 is also provided with a fusel (material R8) extraction port which is mainly rich in fusel such as ethanol, wherein the water content is 70.0%, the extraction temperature is 40 ℃, and the pressure is 1.7kg/cm2. The produced fusel is sent to a fusel tank area through a fifth cooler M23 and a second buffer tank M24 in sequence.
In the above process, the compositions of the relevant materials are shown in table 1.
TABLE 1 composition of materials w%
| Material numbering | R1 | R2 | R3 | R4 | R5 | R6 | R7 | R8 |
| H2 | 0.0011 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| CO | 0.0028 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| CO2 | 2.1701 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Methane | 0.0139 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Ethane (III) | 0.005 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| N2 | 0.0105 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Methanol | 87.9496 | 83.58539 | 70.36215 | 99.99084 | 99.99084 | 99.99411 | 0.172795 | 17.55007 |
| Ethanol | 0.15 | 0.14285 | 0.254428 | 0.004482 | 0.004482 | 0.005685 | 0.021437 | 6.825496 |
| Methyl ether | 0.04 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Pentane (pentane) | 0.00667 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Isopentane | 0.00667 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Octane | 0.00667 | 0 | 0 | 0 | 0 | 0 | 0 | 0 |
| Isobutanol | 0.02925 | 0.027854 | 0.050307 | 6.91E-22 | 6.91E-22 | 1.96E-23 | 0.002096 | 1.398562 |
| Propanol(s) | 0.02925 | 0.027854 | 0.050307 | 7.60E-17 | 7.60E-17 | 5.37E-18 | 0.002151 | 1.398149 |
| N-butanol | 0.02925 | 0.027854 | 0.050307 | 8.80E-28 | 8.80E-28 | 0 | 0.000555 | 1.410152 |
| Pentanol (amyl alcohol) | 0.02925 | 0.027854 | 0.050307 | 0 | 0 | 0 | 0.000185 | 1.412927 |
| Ethyl acetate | 0.028 | 8.12E-10 | 1.10E-13 | 1.63E-09 | 1.63E-09 | 1.58E-13 | 1.26E-26 | 9.85E-25 |
| Acetone (II) | 0.007 | 0.002282 | 0.00014 | 0.004494 | 0.004494 | 0.0002 | 2.80E-16 | 1.12E-12 |
| Water (W) | 9.485 | 16.15806 | 29.18206 | 0.000188 | 0.000188 | 1.77E-07 | 99.80078 | 70.00464 |
In the process, the gas phase heat of the refined methanol extracted from the top of the pressurized rectifying tower M2 is reasonably distributed, the reboiling load of the bottom of the atmospheric rectifying tower M3 is firstly met, the residual heat provides partial heat for the reboiling of the bottom of the pre-rectifying tower M1, the external steam heat required by the reboiling of the bottom of the pre-rectifying tower M1 is reduced, the total energy consumption of the system is effectively reduced, and the equipment investment is reduced. Wherein the heat coupling of the pressurized rectifying tower M2 and the atmospheric rectifying tower M3 is double-effect rectification, and the heat coupling of the pressurized rectifying tower M2 and the pre-rectifying tower M1 is triple-effect rectification.
By adopting the scheme, a certain 60 ten thousand tons/year crude methanol refining factory is improved, and 96.72t/h crude methanol is fed. The purity of refined methanol before modification is 99.9%, the energy consumption of the system is 56.85MKcal/h, the methanol extraction amount is 84.1t/h, and the steam consumption of a single ton of refined methanol is 1.37. The purity of the refined methanol is 99.9 percent after transformation, the energy consumption of the system is 37.8MKcal/h, the extraction amount of the methanol is 84.5t/h, and the steam consumption of a single ton of the refined methanol is 0.89. Intersecting with the traditional process, the energy consumption of the system is reduced by 35 percent.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (8)
1. A three-tower triple-effect crude methanol refining process method is characterized in that after crude methanol enters a pre-rectifying tower, light components and a small amount of gaseous methanol are extracted from the top of the pre-rectifying tower, and aqueous methanol solution A is extracted from the bottom of the pre-rectifying tower and enters a pressurized rectifying tower; the refined methanol gas phase material extracted from the top of the pressurized rectifying tower is divided into two parts: one is sent to the bottom of the atmospheric distillation tower and provides heat required by reboiling for the atmospheric distillation tower, and the other is sent to the bottom of the pre-rectification tower and provides partial heat required by reboiling for the pre-rectification tower; after heat exchange, the two strands of refined methanol gas phase materials become refined methanol condensate respectively and are combined; the combined refined methanol condensate is divided into at least two parts: one as reflux liquid and reflux into the pressurized rectifying tower and the other as product; the aqueous methanol solution B extracted from the bottom of the pressurized rectifying tower enters a normal pressure rectifying tower; the refined methanol gas phase material extracted from the top of the atmospheric distillation tower is divided into two parts: one strand is taken as a product, and the other strand forms reflux liquid and flows back into the normal pressure rectifying tower; waste water materials are extracted from the bottom of the atmospheric distillation tower,
the number of the tower plates of the pre-rectifying tower is 52, the temperature of the extraction at the top of the tower is 64.7 ℃, the pressure is 129kPa, the reflux ratio is 5.5, the extraction temperature at the bottom of the tower is 80.4 ℃, and the pressure is 1.6kg/cm2(ii) a The tower plate number of the pressurized rectifying tower is 85 layers, the temperature extracted from the tower top is 122.6 ℃, and the pressure is 7.0kg/cm2Reflux ratio of 2.2, bottom temperature of 132.7 deg.C and pressure of 7.6kg/cm2(ii) a The number of the tower plates of the atmospheric distillation tower is 90 layers, the temperature extracted from the top of the tower is 72.3 ℃, and the pressure is 1.4kg/cm2Reflux ratio of 1.7, bottom temperature of 114.1 deg.C and pressure of 1.7kg/cm2。
2. The three-tower three-effect crude methanol refining process of claim 1, wherein the feed composition of the crude methanol is: the methanol content is 85-95w%, the light component impurity is 1.5-2.5w%, and the heavy component impurity is 2.5-13.5 w%; the methanol content in the gas phase material extracted from the top of the pre-rectifying tower is 60-65w%, and the methanol content in the aqueous methanol solution A extracted from the bottom of the pre-rectifying tower is 70-85 w%; the content of methanol in the aqueous methanol solution A extracted from the bottom of the pressurized rectifying tower is 70-75 w%.
3. The process for refining the crude methanol by three towers and three effects according to claim 1, wherein the gas phase material extracted from the top of the pre-rectifying tower is subjected to gas-liquid separation after primary condensation and secondary condensation respectively, the separated liquid is taken as reflux liquid and flows back into the pre-rectifying tower, and the separated gas and the non-condensable gas after secondary condensation are combined and sent to a subsequent treatment system.
4. The process of claim 1, wherein the pre-rectifying tower has at least two reboiling units at the bottom, one of which is thermally coupled to one of the streams of the refined methanol gas phase taken from the top of the pressurized rectifying tower.
5. The process of claim 1, wherein the pre-rectifying tower has three reboiling units at the bottom, one of which is thermally coupled to one of the streams of the refined methanol gas phase taken from the top of the pressurized rectifying tower.
6. The process for refining the coarse methanol by three towers and three effects as claimed in claim 1, wherein the refined methanol gas phase material extracted from the top of the pressurized rectifying tower is subjected to heat exchange to become refined methanol condensate and combined, and the non-condensable gas is taken as a third stream and combined with the gas phase material extracted from the top of the atmospheric rectifying tower in a gas form to be extracted.
7. The three-tower three-effect crude methanol refining process method as claimed in claim 1, wherein the refined methanol gas phase material extracted from the top of the atmospheric distillation tower is divided into two parts after being condensed: one strand of the liquid is used as reflux liquid and flows back into a normal pressure rectifying tower; the other is further cooled and withdrawn as product.
8. The three-tower three-effect crude methanol refining process method as claimed in claim 1, wherein fusel alcohol is also extracted from the middle lower part of the atmospheric distillation tower, the water content of the fusel alcohol is 50-80 w%, the extraction temperature is 95-101 ℃, and the pressure is 110-170 KPa.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1600762A (en) * | 2003-09-23 | 2005-03-30 | 上海焦化有限公司 | Method for preparing methyl alcohol in high purity |
| CN1817836A (en) * | 2006-03-10 | 2006-08-16 | 天津大学 | Double-efficient energy-saving and water-saving rectifying system and process for methanol |
| CN1861553A (en) * | 2006-06-13 | 2006-11-15 | 天津大学 | Rectifying tech. and equipment of high purity methanol |
| CN101012150A (en) * | 2007-02-07 | 2007-08-08 | 浙江大学 | Method of refining synthetic methanol with heat integration |
| CN101570466A (en) * | 2009-05-18 | 2009-11-04 | 张君涛 | Multi-effect rectifying process of methanol |
| CN101693645A (en) * | 2009-10-14 | 2010-04-14 | 刘海峰 | Methanol multitower rectifying process and rectifying equipment |
| CN102039058A (en) * | 2010-11-26 | 2011-05-04 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN103539634A (en) * | 2013-10-22 | 2014-01-29 | 四川天一科技股份有限公司 | Method for obtaining fine methanol products by using methanol to olefins (MTO) methanol products |
-
2018
- 2018-06-06 CN CN201810576613.8A patent/CN108558603B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1600762A (en) * | 2003-09-23 | 2005-03-30 | 上海焦化有限公司 | Method for preparing methyl alcohol in high purity |
| CN1817836A (en) * | 2006-03-10 | 2006-08-16 | 天津大学 | Double-efficient energy-saving and water-saving rectifying system and process for methanol |
| CN1861553A (en) * | 2006-06-13 | 2006-11-15 | 天津大学 | Rectifying tech. and equipment of high purity methanol |
| CN101012150A (en) * | 2007-02-07 | 2007-08-08 | 浙江大学 | Method of refining synthetic methanol with heat integration |
| CN101570466A (en) * | 2009-05-18 | 2009-11-04 | 张君涛 | Multi-effect rectifying process of methanol |
| CN101693645A (en) * | 2009-10-14 | 2010-04-14 | 刘海峰 | Methanol multitower rectifying process and rectifying equipment |
| CN102039058A (en) * | 2010-11-26 | 2011-05-04 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN103539634A (en) * | 2013-10-22 | 2014-01-29 | 四川天一科技股份有限公司 | Method for obtaining fine methanol products by using methanol to olefins (MTO) methanol products |
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