CN222534119U - Crude methanol refining device with high water content - Google Patents
Crude methanol refining device with high water content Download PDFInfo
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- CN222534119U CN222534119U CN202420945738.4U CN202420945738U CN222534119U CN 222534119 U CN222534119 U CN 222534119U CN 202420945738 U CN202420945738 U CN 202420945738U CN 222534119 U CN222534119 U CN 222534119U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 342
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 238000007670 refining Methods 0.000 title claims abstract description 25
- 238000010992 reflux Methods 0.000 claims abstract description 216
- 238000000605 extraction Methods 0.000 claims abstract description 152
- 230000018044 dehydration Effects 0.000 claims abstract description 149
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 149
- 239000012071 phase Substances 0.000 claims description 80
- 239000007791 liquid phase Substances 0.000 claims description 60
- 238000003808 methanol extraction Methods 0.000 claims description 27
- 239000002351 wastewater Substances 0.000 claims description 15
- 238000004821 distillation Methods 0.000 abstract description 31
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 17
- 230000008878 coupling Effects 0.000 abstract description 4
- 238000010168 coupling process Methods 0.000 abstract description 4
- 238000005859 coupling reaction Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 71
- 239000000463 material Substances 0.000 description 26
- 239000000047 product Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 10
- 238000010438 heat treatment Methods 0.000 description 7
- 239000002994 raw material Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001944 continuous distillation Methods 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
本申请提供了一种高水含量粗甲醇精制装置，包括预精馏塔、脱水精馏塔、负压精馏塔、精馏塔一、精馏塔二，脱水精馏塔的顶部通过脱水塔气相采出管线与脱水塔再沸器连接，脱水塔气相采出管线上设置有压缩机，脱水塔再沸器的输出端与脱水塔回流罐连接，脱水塔回流罐的底部设置有脱水塔回流罐采出管线，脱水塔回流罐采出管线分别与脱水塔回流管线、负压塔进料管线连接，脱水塔回流管线与脱水精馏塔的上部连接，负压塔进料管线与负压精馏塔连接；本申请能够对高水含量粗甲醇进行精制，保证最终甲醇产品的精度，且保证甲醇产品＞99.99％的同时，蒸汽单耗≤0.7t蒸汽/t精醇，降低了系统的蒸汽消耗，实现能量多级利用和热量耦合。
The present application provides a crude methanol refining device with high water content, comprising a pre-distillation tower, a dehydration distillation tower, a negative pressure distillation tower, a distillation tower 1 and a distillation tower 2, wherein the top of the dehydration distillation tower is connected to the dehydration tower reboiler through a dehydration tower gas phase extraction pipeline, a compressor is arranged on the dehydration tower gas phase extraction pipeline, the output end of the dehydration tower reboiler is connected to the dehydration tower reflux tank, a dehydration tower reflux tank extraction pipeline is arranged at the bottom of the dehydration tower reflux tank, the dehydration tower reflux tank extraction pipeline is respectively connected to the dehydration tower reflux pipeline and the negative pressure tower feed pipeline, the dehydration tower reflux pipeline is connected to the upper part of the dehydration distillation tower, and the negative pressure tower feed pipeline is connected to the negative pressure distillation tower; the present application can purify crude methanol with high water content, ensure the accuracy of the final methanol product, and ensure that the methanol product is greater than 99.99%, while the steam unit consumption is ≤0.7t steam/t refined alcohol, thereby reducing the steam consumption of the system and realizing multi-stage energy utilization and heat coupling.
Description
Technical Field
The application relates to the technical field of crude methanol refining, in particular to a high-water-content crude methanol refining device.
Background
The coal chemical industry plays an important role in sustainable utilization of Chinese energy, the novel coal chemical industry faces new market demands and development opportunities in China, methanol downstream products such as coal olefins and the like are rapidly developed, in order to ensure that high-water-content crude alcohol refining is more excellent in economical efficiency, high efficiency and energy conservation, and can adapt to unstable fluctuation of markets, the aim of optimal quality, lowest energy consumption and maximum economic benefit of AA-grade methanol products is achieved, energy conservation and controllability are achieved under the minimum investment, the light components in the methanol are mainly removed through a stabilizer or a pre-tower in the current production process, the light components are fed into a methanol rectifying device, the energy consumption and the investment are relatively high, the energy consumption for producing single ton of refined methanol is about 1.5t, along with the technical development, the existing technology can realize lower energy consumption for producing single ton of refined methanol, but is only applicable to low-water-content crude methanol, the final methanol purity obtained in the technology is lower, and the closest existing technology is retrieved as follows:
The five-tower four-effect crude methanol refining process and equipment with the patent application number of CN202310877976.6 comprise a prefractionation tower, a negative pressure rectification tower, a pressurizing rectification tower, a normal pressure rectification tower and a recovery tower, the mode of thermal coupling and heat pump combination is adopted, for the stock market, the purposes that the traditional three-tower methanol rectifying process can be expanded by more than 30 percent and the steam consumption is reduced by 45 to 50 percent can be achieved, for the new market, the investment is small, the operability is strong, energy-saving measures such as heat recycling and the like are adopted by adopting a heat exchange network, the steam consumption is greatly reduced, the methanol consumption per ton can be reduced to below 0.5 ton of steam, the steam consumption per ton of methanol can be reduced to below 0.5 ton of steam, the very low steam consumption is guaranteed, but the methanol is not dehydrated in the application, the application is only suitable for treating the crude methanol with low water content, the crude methanol with the high water content is treated, the crude methanol with the water content of 3.8 percent in the second embodiment of the application description, the application is low water content of the crude methanol with the water content of 3.8 percent, the product with the water content of the crude methanol with the high water content of the methanol content of the product with the high water content of the methanol content of 3.95 ppm can be obtained by the crude methanol with the high water content of the product with the water content of the crude methanol with the water content of 3.95 ppm, and the product with the water content of the crude methanol with the water content of the product is obtained after the crude methanol is treated is relatively high, and the crude product is obtained, and has the product purity is higher purity is obtained, and has the purity is only is higher is obtained, and has the product purity is higher purity is obtained.
In summary, it is desirable to provide a refining apparatus that is capable of refining high water content crude methanol to ensure a minimum steam consumption while ensuring a higher purity of the methanol product.
Disclosure of Invention
The application provides a high-water-content crude methanol refining device which comprises a pre-rectifying tower, a dehydration rectifying tower, a negative pressure rectifying tower, a rectifying tower I and a rectifying tower II which are sequentially connected, wherein a dehydration tower gas phase extraction pipeline is arranged at the top of the dehydration rectifying tower and is connected with a dehydration tower reboiler, a compressor is arranged on the dehydration tower gas phase extraction pipeline, the output end of the dehydration tower reboiler is connected with a dehydration tower reflux tank through a dehydration tower reboiler output pipeline, a dehydration tower top condenser is arranged on the dehydration tower reboiler output pipeline, a dehydration tower reflux tank extraction pipeline is arranged at the bottom of the dehydration tower reflux tank and is connected with a dehydration tower reflux pipeline and a negative pressure tower feeding pipeline respectively, and the dehydration tower reflux pipeline is connected with the upper part of the dehydration rectifying tower and the negative pressure tower feeding pipeline is connected with the negative pressure rectifying tower.
As a preferred scheme, the dehydration column reboiler output line passes through a pre-column steam reboiler.
As a preferable scheme, the top of the pre-rectifying tower is connected with a negative pressure tower reboiler I through a pre-tower top extraction pipeline, the output end of the negative pressure tower reboiler I is connected with a pre-tower buffer tank through a negative pressure tower reboiler I output pipeline, a pre-tower reflux pipeline is arranged at the bottom of the pre-tower buffer tank, an extraction water pipeline is arranged at one side of the pre-tower buffer tank, and a pre-tower buffer tank gas-phase extraction pipeline is arranged at the upper part of the pre-tower buffer tank.
As a preferable scheme, the bottom of the pre-rectifying tower is connected with the dehydration rectifying tower through a pre-tower kettle extraction pipeline, a pre-tower kettle pump and a dehydration tower feeding preheater are arranged on the pre-tower kettle extraction pipeline, the tower kettle of the dehydration rectifying tower extracts waste water through the dehydration tower kettle extraction pipeline, and the dehydration tower kettle extraction pipeline passes through the dehydration tower feeding preheater.
As a preferable mode, the dehydration rectifying tower adopts a negative pressure rectifying tower or an atmospheric rectifying tower.
The top of the negative pressure rectifying tower is connected with a negative pressure tower reflux tank through a negative pressure tower top extraction pipeline, a negative pressure tower top condenser is arranged on the negative pressure tower top extraction pipeline, a negative pressure tower reflux tank liquid phase pipeline is arranged at the lower part of the negative pressure tower reflux tank, a negative pressure tower reflux pump is arranged on the negative pressure tower reflux tank liquid phase pipeline, the negative pressure tower reflux tank liquid phase pipeline is respectively connected with the negative pressure tower reflux pipeline and the negative pressure tower refined methanol extraction pipeline, the negative pressure tower reflux pipeline is connected with the upper part of the negative pressure rectifying tower, a negative pressure tower reflux tank gas phase extraction pipeline is arranged at the upper part of the negative pressure tower reflux tank, and a negative pressure tower top secondary condenser and a vacuum pump are arranged on the negative pressure tower reflux tank gas phase extraction pipeline.
As a preferable scheme, the refined methanol extraction pipeline of the negative pressure tower is connected with a refined methanol tank.
The method comprises the steps of adopting an atmospheric rectifying tower I and an atmospheric rectifying tower II respectively, connecting the top of the atmospheric rectifying tower with a negative pressure tower reboiler II through an atmospheric tower gas phase extraction pipeline, connecting the output end of the negative pressure tower reboiler II with an atmospheric tower reflux tank, arranging an atmospheric tower reflux tank liquid phase extraction pipeline at the bottom of the atmospheric tower reflux tank, respectively connecting the atmospheric tower reflux pipeline and an atmospheric tower refined methanol extraction pipeline with the atmospheric tower liquid phase extraction pipeline, connecting the atmospheric tower reflux pipeline with the upper part of the atmospheric rectifying tower, respectively connecting the top of the atmospheric rectifying tower with a pre-tower reboiler and an atmospheric tower reboiler through an atmospheric tower gas phase extraction pipeline, respectively connecting the output end of the pre-tower reboiler and the output end of the atmospheric tower reboiler with an atmospheric tower reflux tank, and arranging an atmospheric tower reflux tank liquid phase extraction pipeline at the bottom of the atmospheric tower reflux tank, respectively connecting the atmospheric tower reflux pipeline and the atmospheric tower refined methanol extraction pipeline with the atmospheric tower reflux pipeline, wherein the atmospheric tower reflux pipeline is connected with the upper part of the atmospheric rectifying tower.
As a preferable scheme, the refined methanol extraction pipeline of the atmospheric tower is connected with a refined methanol tank.
As a preferable scheme, the refined methanol extraction pipeline of the pressurizing tower is connected with the refined methanol tank.
As a preferable scheme, the tower bottom of the negative pressure rectifying tower is connected with the normal pressure rectifying tower through a negative pressure tower bottom extraction pipeline, and the negative pressure tower bottom extraction pipeline is provided with a negative pressure tower bottom pump and a normal pressure tower feeding preheater.
As a preferable scheme, the bottom of the normal pressure rectifying tower is connected with the pressurized rectifying tower through a normal pressure tower kettle extraction pipeline, a normal pressure tower kettle pump, a pressurized tower primary feed preheater and a pressurized tower secondary feed preheater are arranged on the normal pressure tower kettle extraction pipeline, the pressurized rectifying tower kettle is provided with a pressurized tower kettle extraction pipeline, the pressurized tower kettle extraction pipeline extracts wastewater, and the pressurized tower kettle extraction pipeline passes through the pressurized tower primary feed preheater.
As a preferable scheme, a steam pipeline sequentially passes through a pressurizing tower reboiler, a pressurizing tower secondary feed preheater, an atmospheric tower feed preheater and a pre-tower feed preheater, and the output end of the pre-tower feed preheater is connected with a condensate pipeline.
The first rectifying tower and the rectifying tower adopt a pressurized rectifying tower and an atmospheric rectifying tower respectively, the top of the pressurized rectifying tower is connected with a pre-tower reboiler and an atmospheric tower reboiler respectively through a pressurized tower gas phase extraction pipeline, the output end of the pre-tower reboiler and the output end of the atmospheric tower reboiler are both connected with a pressurized tower reflux tank, the bottom of the pressurized tower reflux tank is provided with a pressurized tower reflux tank liquid phase extraction pipeline, the pressurized tower reflux tank liquid phase extraction pipeline is connected with a pressurized tower reflux pipeline and a pressurized tower refined methanol extraction pipeline respectively, wherein the pressurized tower reflux pipeline is connected with the middle upper part of the pressurized rectifying tower, the top of the atmospheric rectifying tower is connected with a negative pressure tower reboiler through an atmospheric tower gas phase extraction pipeline, the output end of the negative pressure tower reboiler is connected with an atmospheric tower reflux tank respectively, the bottom of the atmospheric tower reflux tank is provided with an atmospheric tower reflux tank liquid phase extraction pipeline, and the atmospheric tower refined methanol extraction pipeline are connected with the atmospheric tower reflux pipeline respectively, and the atmospheric tower reflux pipeline are connected with the upper part of the rectifying tower.
As a preferable scheme, the refined methanol extraction pipeline of the atmospheric tower is connected with a refined methanol tank.
As a preferable scheme, the refined methanol extraction pipeline of the pressurizing tower is connected with the refined methanol tank.
As a preferred scheme, the tower kettle of negative pressure rectifying column is connected with the pressurization rectifying column through negative pressure tower kettle extraction pipeline, negative pressure tower kettle extraction pipeline is provided with negative pressure tower kettle pump, pressurization tower one-level feeding preheater, pressurization tower second grade feeding preheater, the tower kettle of pressurization rectifying column is provided with pressurization tower kettle extraction pipeline, and pressurization tower kettle extraction pipeline is connected with the well upper portion of ordinary pressure rectifying column, and pressurization tower kettle extraction pipeline is through pressurization tower one-level feeding preheater.
As a preferable scheme, a steam pipeline sequentially passes through a pressurizing tower reboiler, a pressurizing tower secondary feeding preheater and a pre-tower feeding preheater, and the output end of the pre-tower feeding preheater is connected with a condensate pipeline.
According to the application, the dehydration rectifying tower is arranged, so that the high-water-content crude methanol can be refined, the energy at the top of the dehydration rectifying tower is fully recycled through the compressor (heat pump) and is used for providing heat for the reboiler of the dehydration rectifying tower, the distillate at the bottom of the dehydration rectifying tower is heated, and the materials subjected to heat exchange with the reboiler of the dehydration rectifying tower are not directly extracted and directly enter the negative pressure rectifying tower, but are treated by the reflux tank of the dehydration rectifying tower, and then are partially refluxed to the dehydration rectifying tower, and partially enter the negative pressure rectifying tower, so that the accuracy of subsequent distillation is further ensured, and the accuracy of a final methanol product is further ensured; the application can be used for converting the low-grade heat at the top of the dehydration rectifying tower into high-grade heat to meet the heat requirement of a reboiler of the dehydration rectifying tower, and for crude methanol with the water content of 35 percent, the methanol content after dehydration can reach 91 percent, the methanol purity after refining is 99.99 percent, the ethanol content in refined methanol is less than or equal to 50ppm, and the methanol content in waste water is less than or equal to 10ppm, thereby being capable of reaching the standard and being discharged.
In addition, the application has the following advantages:
1. The steam at the top of the pre-rectifying tower supplies heat for the reboiler of the negative pressure tower, provides heat for the distillation of the negative pressure rectifying tower, fully utilizes the heat of the steam at the top of the pre-rectifying tower, saves the steam of the negative pressure rectifying tower, reduces the steam consumption of a system, does not need to adopt circulating water cooling at the top of the pre-rectifying tower, and saves a large amount of circulating water;
2. The method fully utilizes the steam heat of the first rectifying tower and the second rectifying tower, when the first rectifying tower and the rectifying tower adopt an atmospheric rectifying tower and a pressurized rectifying tower respectively, the steam at the top of the atmospheric rectifying tower provides heat for a reboiler II of the negative pressure tower, so as to provide heat required by distillation for the negative pressure rectifying tower, and the heat at the top of the atmospheric rectifying tower is utilized, thereby saving the steam of the negative pressure rectifying tower;
When the first rectifying tower and the rectifying tower respectively adopt a pressurized rectifying tower and an atmospheric rectifying tower, the steam at the top of the pressurized rectifying tower provides heat for a pre-rectifying tower reboiler and an atmospheric rectifying tower reboiler, and further provides heat required by distillation for the pre-rectifying tower and the atmospheric rectifying tower, the heat at the top of the pressurized rectifying tower is utilized, the steam of the pre-rectifying tower and the atmospheric rectifying tower is saved, the steam at the top of the atmospheric rectifying tower provides heat for a negative pressure rectifying tower reboiler II, and further provides heat required by distillation for the negative pressure rectifying tower, the heat at the top of the atmospheric rectifying tower is utilized, and the steam of the negative pressure rectifying tower is saved;
3. When the first rectifying tower and the rectifying tower adopt an atmospheric rectifying tower and a pressurizing rectifying tower respectively, the materials in the tower kettle of the pressurizing rectifying tower provide heat for a first-stage feeding preheater of the pressurizing tower, and steam is adopted as condensate after the heat is provided by a reboiler of the pressurizing tower, a second-stage feeding preheater of the pressurizing tower, a feeding preheater of the atmospheric tower and a feeding preheater of the pre-tower in sequence;
When the first rectifying tower and the rectifying tower adopt a pressurized rectifying tower and an atmospheric rectifying tower respectively, the materials at the bottom of the pressurized rectifying tower are sent to a first-stage feeding preheater of the pressurized tower, heat required for heating the materials is provided for the first-stage feeding preheater of the pressurized tower and then enter the atmospheric rectifying tower;
4. The application fully utilizes the heat of the tower top of each tower and the residual heat of the tower kettle condensate and the steam condensate, ensures that the unit steam consumption is less than or equal to 0.7t steam/t refined alcohol while ensuring that the methanol product is more than 99.99 percent, greatly reduces the steam consumption of the system and realizes the multi-stage utilization of energy and the heat coupling;
5. The water content and the alcohol content in the refined methanol obtained by the method can be freely regulated and controlled, and the wastewater can be discharged up to the standard without further treatment.
Drawings
FIG. 1 is a schematic view of a first embodiment of the present application;
FIG. 2 is a schematic diagram of a second embodiment of the present application;
1. A pre-tower feed preheater; 2, a pre-rectifying tower; 3, a negative pressure tower reboiler I; the method comprises the steps of 4, a negative pressure rectifying tower, 5, a pre-tower buffer tank, 6, a gas phase extraction pipeline, 7, a dehydration rectifying tower, 8, a dehydration tower feeding preheater, 9, a compressor, 10, a dehydration tower reboiler, 11, a pre-tower steam reboiler, 12, a dehydration tower overhead condenser, 13, a dehydration tower reflux drum, 14, a normal pressure tower feeding preheater, 15, a normal pressure rectifying tower, 16, a negative pressure tower reboiler II, 17, a normal pressure tower reflux drum, 18, a refined methanol tank, 19, a pressurization tower primary feeding preheater, 20, a pressurization tower secondary feeding preheater, 25, a pressurization tower reboiler, 26, a pre-tower reboiler, 27, a pre-tower tank pump, 28, a negative pressure tower tank outlet pipeline, 29, a negative pressure tower tank pump, 30, a normal pressure tower tank outlet pipeline, 31, a normal pressure tower pump, 32, a pressurization tower tank outlet, 33, a dehydration tower reboiler, 34, a dehydration tower reboiler, a negative pressure tower outlet, a negative pressure tower, a negative pressure pump, a negative pressure tower outlet, a negative pressure pump, a negative pressure tower reflux drum, a negative pressure pump, a negative pressure tower top portion, a negative pressure pump, a negative pressure tower reflux drum, a negative pressure pump, a negative pressure tower, a negative pressure pipeline, a negative pressure tower, a negative pressure tank, a negative pressure pipeline, a negative pressure tank, a pressure pipeline, a pressure pipeline, and a pressure pipeline, and a pressure pipelines, and a pipeline, and a vacuum pipeline, and a vacuum pipeline vacuum pipeline, and vacuum pipeline, and vacuum, vacuum tower, and vacuum, and, and, the method comprises the steps of normal pressure tower reflux tank liquid phase extraction pipelines, 54 normal pressure tower reflux pumps, 55 normal pressure tower reflux pipelines, 56 normal pressure tower refined methanol extraction pipelines, 57 pressurized tower gas phase extraction pipelines, 58 pressurized tower reflux tank liquid phase extraction pipelines, 59 pressurized tower reflux pumps, 60 pressurized tower reflux pipelines, 61 pressurized tower refined methanol extraction pipelines, 62, steam pipelines, 63, condensate pipelines, 64, pressurized tower kettle pumps, 65, dehydration tower kettle extraction pipelines, 66, negative pressure tower top secondary condensers and 67, and vacuum pumps.
Detailed Description
The following describes the embodiments of the present invention in detail with reference to fig. 1 and 2. It should be noted that the detailed description herein is presented for purposes of illustration and explanation only and is not intended to limit the invention.
Embodiment one:
The embodiment provides a high-water-content crude methanol refining device, which comprises a pre-rectifying tower 2, a dehydration rectifying tower 7, a negative pressure rectifying tower 4, a rectifying tower I and a rectifying tower II which are sequentially connected, wherein the dehydration rectifying tower 7 adopts a negative pressure rectifying tower or an atmospheric rectifying tower, the rectifying tower I and the rectifying tower respectively adopt an atmospheric rectifying tower 15 and a pressurizing rectifying tower 21 in the embodiment, a pre-tower steam reboiler 11 and a pre-tower reboiler 22 are arranged at the lower part of the pre-rectifying tower 2, a dehydration tower reboiler 10 is arranged at the lower part of the dehydration rectifying tower 7, a negative pressure tower reboiler 3 and a negative pressure tower reboiler 16 are arranged at the lower part of the negative pressure rectifying tower 4, an atmospheric reboiler 24 is arranged at the lower part of the atmospheric rectifying tower 15, and a pressurizing tower reboiler 25 is arranged at the lower part of the pressurizing rectifying tower 21;
The bottom of the pre-rectifying tower 2 is connected with a dehydration rectifying tower 7 through a pre-tower kettle extraction pipeline 26, the dehydration rectifying tower 7 is used for dehydrating crude methanol with high water content, a pre-tower kettle pump 27 and a dehydration tower feed preheater 8 are arranged on the pre-tower kettle extraction pipeline 26, a dehydration tower gas phase extraction pipeline 33 is arranged at the top of the dehydration rectifying tower 7, the dehydration tower gas phase extraction pipeline 33 is connected with a dehydration tower reboiler 10, a compressor 9 is arranged on the dehydration tower gas phase extraction pipeline 33, the gas phase at the top of the dehydration rectifying tower 7 is pressurized and heated by the compressor 9 to provide heat for the dehydration tower reboiler 10, the output end of the dehydration tower reboiler 10 is connected with a dehydration tower reflux drum 13 through a dehydration tower reboiler output pipeline 34, preferably, a dehydration tower condenser 12 is arranged on the dehydration tower reboiler output pipeline 34 passes through a pre-tower steam 11, a material dehydration tower 7 is subjected to a dehydration feed preheater 8, a dehydration tower feed preheater 8 is provided with a heater, the heat required by the dehydration tower reboiler is further connected with a dehydration tower reflux drum 7, a reflux drum 35 is connected with a reflux drum 37, a negative pressure reflux drum 35 is arranged at the bottom of the reflux drum 7, a reflux drum is connected with a reflux drum 3, and a reflux drum is connected with a reflux drum 3, a reflux drum is connected with a reflux drum 3 through a reflux drum 37, the material at the tower bottom of the pre-rectifying tower 2 enters the dewatering rectifying tower 7 after being preheated by the dewatering tower feeding preheater 8, the gas phase at the top of the dewatering rectifying tower 7 is pressurized and heated by the compressor 9 to sequentially provide heat for the dewatering tower reboiler 10 and the pre-tower steam reboiler 11, then the gas phase is condensed by the dewatering tower top condenser 12 and enters the dewatering tower reflux tank 13, the liquid phase in the dewatering tower reflux tank 13 is partially refluxed to the dewatering rectifying tower 7 and partially enters the negative pressure rectifying tower 4, the dewatering rectifying tower 7 can refine crude methanol with high water content, the energy at the tower top of the dewatering rectifying tower 7 is fully recycled by the compressor 9 and is used for providing heat for the dewatering tower reboiler 10, the distillate at the tower bottom of the dewatering rectifying tower 7 is heated, the material after heat exchange with the dewatering tower reboiler is not directly extracted, and also does not directly enter the negative pressure rectifying tower 4, but is partially refluxed to the dewatering rectifying tower 7 after being treated by the dewatering tower reflux tank, and partially enters the negative pressure rectifying tower 4, and further ensures the precision of the final distilled product;
The top of the negative pressure rectifying tower 4 is connected with a negative pressure tower reflux drum 46 through a negative pressure tower top extraction pipeline 45, a negative pressure tower top condenser 47 is arranged on the negative pressure tower top extraction pipeline 45, a negative pressure tower reflux drum liquid phase pipeline 48 is arranged on the lower part of the negative pressure tower reflux drum 46, a negative pressure tower reflux drum liquid phase pipeline 48 is arranged on the negative pressure tower reflux drum liquid phase pipeline 48, the negative pressure tower reflux drum liquid phase pipeline 48 is respectively connected with a negative pressure tower reflux pipeline 50 and a negative pressure tower rectifying methanol extraction pipeline 51, wherein the negative pressure tower reflux pipeline 50 is connected with the upper part of the negative pressure rectifying tower 4, the negative pressure tower rectifying methanol extraction pipeline 51 is connected with a rectifying methanol tank 18, the upper part of the negative pressure tower reflux drum 46 is provided with a negative pressure tower reflux drum gas phase extraction pipeline 52, the negative pressure tower reflux drum gas phase extraction pipeline 52 is provided with a negative pressure tower secondary condenser 66 and a vacuum pump 67, the tower kettle of the negative pressure rectifying tower 4 is connected with a negative pressure tower 15 through a negative pressure tower top pre-heater 28, the negative pressure tower bottom tower liquid phase pipeline 28 is provided with a negative pressure tower bottom tower pre-heater 29, the gas phase 14 enters the rectifying tower top of the rectifying tower 4 after the negative pressure tower is fed into the rectifying tower 14, and the negative pressure tower top of the rectifying tower 4 is fed into the negative pressure tower top of the rectifying tower 18, and the rectifying tower is fed into the negative pressure tower 4 through the negative pressure tower top of the negative pressure tower 18, the negative pressure tower top of the rectifying tower is fed into the negative pressure tower 18, the rectifying tower is fed into the rectifying tower top of the rectifying tower 18, the rectifying tower is partially the rectifying tower is treated by the negative pressure tower top of the rectifying tower and the rectifying tower 4, the rectifying tower is fed into the rectifying tower and the rectifying tower tank is fed into the rectifying tower and the rectifying tower;
The bottom of the normal pressure rectifying tower 15 is connected with the pressurizing rectifying tower 21 through a normal pressure tower kettle extraction pipeline 30, a normal pressure tower kettle pump 31, a pressurizing tower primary feed preheater 19 and a pressurizing tower secondary feed preheater 20 are arranged on the normal pressure tower kettle extraction pipeline 30, miscellaneous alcohol is extracted from the side line of the pressurizing rectifying tower 21, a pressurizing tower kettle extraction pipeline 32 is arranged on the pressurizing rectifying tower 21, a pressurizing tower kettle pump 64 is arranged on the pressurizing tower kettle extraction pipeline 32, waste water is extracted from the pressurizing tower kettle extraction pipeline 32, the pressurizing tower kettle extraction pipeline 32 passes through the pressurizing tower primary feed preheater 19, and materials extracted from the pressurizing rectifying tower 21 enter the pressurizing tower primary feed preheater 19 to provide heat required for heating the materials and then are discharged as waste water.
Preferably, the embodiment fully utilizes the heat of the tops of the pre-rectifying tower 2, the first rectifying tower and the second rectifying tower, the heat of the bottoms of the pre-rectifying tower 2, the first rectifying tower and the second rectifying tower and the waste heat of the steam condensate, and specifically:
The top of the pre-rectifying tower 2 is connected with a negative pressure tower reboiler I3 through a pre-tower top extraction pipeline 39, the output end of the negative pressure tower reboiler I3 is connected with a pre-rectifying tower buffer tank 5 through a negative pressure tower reboiler I output pipeline 40, the bottom of the pre-rectifying tower buffer tank 5 is provided with a pre-tower reflux pipeline 41, the pre-tower reflux pipeline 41 is connected with the upper part of the pre-rectifying tower 2, the pre-rectifying tower reflux pipeline 41 is provided with a pre-tower reflux pump 42, one side of the pre-rectifying tower buffer tank 5 is connected with an extraction water pipeline 43, the upper part of the pre-rectifying tower buffer tank 5 is provided with a gas phase extraction pipeline 6, after the gas phase at the top of the pre-rectifying tower 2 exchanges heat with the negative pressure tower reboiler I3, the gas phase enters the pre-rectifying tower buffer tank 5, the extraction water is introduced into the pre-rectifying tower buffer tank 5, and the liquid phase is extracted through the gas phase extraction pipeline 41, and the gas phase at the top of the pre-rectifying tower 2 is heated against the negative pressure tower reboiler I3, the heat of the pre-rectifying tower 2 is fully utilized, the heat of the pre-rectifying tower 4 is saved, and the circulating water is not required to be cooled by the circulating water again through the water cooling circulation;
The top of the normal pressure rectifying tower 15 is connected with a second negative pressure tower reboiler 16 through a normal pressure tower gas phase extraction pipeline 44, the output end of the second negative pressure tower reboiler 16 is connected with a normal pressure tower reflux tank 17, the bottom of the normal pressure tower reflux tank 17 is provided with a normal pressure tower reflux tank liquid phase extraction pipeline 53, the normal pressure tower reflux tank liquid phase extraction pipeline 53 is provided with a normal pressure tower reflux pump 54, the normal pressure tower reflux tank liquid phase extraction pipeline 53 is respectively connected with a normal pressure tower reflux pipeline 55 and a normal pressure tower rectifying methanol extraction pipeline 56, the normal pressure tower reflux pipeline 55 is connected with the upper part of the normal pressure rectifying tower 15, the normal pressure tower rectifying methanol extraction pipeline 56 is connected with a rectifying methanol tank 18, the gas phase at the top of the normal pressure rectifying tower 15 is subjected to heat exchange with the second negative pressure tower reboiler 16 and then enters the normal pressure tower reflux tank 17, and part of the liquid phase of the normal pressure tower reflux tank 17 is extracted into the rectifying methanol tank 18;
The top of the pressurizing rectifying tower 21 is respectively connected with the pre-tower reboiler 22 and the normal pressure tower reboiler 24 through a pressurizing tower gas phase extraction pipeline 57, the output end of the pre-tower reboiler 22 and the output end of the normal pressure tower reboiler 24 are respectively connected with the pressurizing tower reflux tank 23, a pressurizing tower reflux tank liquid phase extraction pipeline 58 is arranged at the bottom of the pressurizing tower reflux tank 23, a pressurizing tower reflux pump 59 is arranged on the pressurizing tower reflux tank liquid phase extraction pipeline 58, the pressurizing tower reflux tank liquid phase extraction pipeline 58 is respectively connected with the pressurizing tower reflux pipeline 60 and the pressurizing tower rectifying methanol extraction pipeline 61, wherein the pressurizing tower reflux pipeline 60 is connected with the upper part of the pressurizing rectifying tower 21, the pressurizing tower rectifying methanol extraction pipeline 61 is connected with the rectifying methanol tank 18, the gas phase at the top of the pressurizing rectifying tower 21 is respectively the pre-tower reboiler 22 and the normal pressure tower reboiler 24, and then enters the pressurizing tower reflux tank 23, and the liquid phase part in the pressurizing tower reflux tank 23 is refluxed to the pressurizing rectifying tower 21, and part of the liquid phase part of the pressurizing tower reflux tank is extracted into the rectifying methanol tank 18;
The pressurizing tower reboiler 25 supplies heat through steam, a steam pipeline 62 sequentially passes through the pressurizing tower reboiler 25, the pressurizing tower secondary feed preheater 20, the atmospheric tower feed preheater 14 and the pre-tower feed preheater 1, and the output end of the pre-tower feed preheater 1 is connected with a condensate pipeline 63, namely the pressurizing tower secondary feed preheater 20 adopts the steam condensate preheating of the pressurizing tower reboiler 25, the atmospheric tower feed preheater 14 adopts the steam condensate preheating of the pressurizing tower secondary feed preheater 20, and the pre-tower feed preheater 1 adopts the steam condensate preheating of the atmospheric tower feed preheater 14, so that the consumption of steam is reduced.
Embodiment two:
the present embodiment provides a refining apparatus for crude methanol with high water content, which is different from the first embodiment in that in the present embodiment, a pressurizing rectifying tower 21 and an atmospheric rectifying tower 15 are respectively adopted in the rectifying tower I and the rectifying tower II;
The bottom of the pre-rectifying tower 2 is connected with the dewatering rectifying tower 7 through a pre-tower kettle extraction pipeline 26, a pre-tower kettle pump 27 and a dewatering tower feed preheater 8 are arranged on the pre-tower kettle extraction pipeline 26, a dewatering tower gas phase extraction pipeline 33 is arranged at the top of the dewatering rectifying tower 7, the dewatering tower gas phase extraction pipeline 33 is connected with a dewatering tower reboiler 10, a compressor 9 is arranged on the dewatering tower gas phase extraction pipeline 33, the gas phase at the top of the dewatering rectifying tower 7 is pressurized and heated by the compressor 9 to provide heat for the dewatering tower reboiler 10, the output end of the dewatering tower reboiler 10 is connected with a dewatering tower reflux drum 13 through a dewatering tower reboiler output pipeline 34, a dewatering tower top condenser 12 is arranged on the dewatering tower reboiler output pipeline 34, preferably, the dewatering tower reboiler output pipeline 34 passes through the pre-tower steam reboiler 11, the material dewatering tower kettle material dewatering tower feed preheater 8 is provided with heat required for heating the dewatering tower feed preheater 8, consumption of external steam is further saved, the dewatering tower kettle 7 is fully utilized, the heat of the dewatering tower kettle 7 is fully utilized, the dewatering tower top is connected with a dewatering tower reflux drum 35, a dewatering tower reflux drum 35 is connected with a dewatering tower reflux drum 3 through a dewatering tower reflux drum 35, a dewatering tower reflux drum 35 is arranged at the bottom of the dewatering tower reflux drum 7, a reflux drum is connected with a dewatering tower reflux drum 3, a reflux drum 3 is arranged at the reflux drum 3, and a reflux drum is connected with a reflux drum 3, a reflux drum is connected with a reflux drum 3 through a reflux drum 3, and a reflux drum is connected with a reflux drum 3 through a reflux drum 3, the material in the tower kettle of the pre-rectifying tower 2 enters the dewatering rectifying tower 7 after being preheated by the dewatering tower feeding preheater 8, the gas phase at the top of the dewatering rectifying tower 7 is pressurized and heated by the compressor 9 to provide heat for the dewatering tower reboiler 10, then enters the dewatering tower feeding preheater 8 to provide heat for the dewatering tower feeding preheater 8, then enters the dewatering tower reflux tank 13 after being condensed by the dewatering tower top condenser 12, and the liquid phase in the dewatering tower reflux tank 13 is partially refluxed to the dewatering rectifying tower 7, and partially enters the negative pressure rectifying tower 4 for continuous distillation, wherein the dewatering rectifying tower 7 can refine crude methanol with high water content, the energy at the top of the dewatering rectifying tower 7 is fully recycled by the compressor 9 for providing heat for the dewatering tower reboiler 10, the distillate at the tower kettle of the dewatering rectifying tower 7 is heated, and the material after heat exchange with the dewatering tower reboiler is not directly extracted, and also does not directly enter the negative pressure rectifying tower 4, but is partially refluxed to the dewatering rectifying tower 7 after being treated by the dewatering tower reflux tank, and partially enters the negative pressure rectifying tower 4, and further ensures the precision of the final distilled product;
The top of the negative pressure rectifying tower 4 is connected with a negative pressure tower reflux tank 46 through a negative pressure tower top extraction pipeline 45, a negative pressure tower top condenser 47 is arranged on the negative pressure tower top extraction pipeline 45, a negative pressure tower reflux tank liquid phase pipeline 48 is arranged at the lower part of the negative pressure tower reflux tank 46, a negative pressure tower reflux pump 49 is arranged on the negative pressure tower reflux tank liquid phase pipeline 48, the negative pressure tower reflux tank liquid phase pipeline 48 is respectively connected with a negative pressure tower reflux pipeline 50 and a negative pressure tower refined methanol extraction pipeline 51, wherein the negative pressure tower reflux pipeline 50 is connected with the upper part of the negative pressure rectifying tower 4, and the negative pressure tower refined methanol extraction pipeline 51 is connected with the refined methanol tank 18; the upper part of the negative pressure tower reflux tank 46 is provided with a negative pressure tower reflux tank gas phase extraction pipeline 52, the negative pressure tower reflux tank gas phase extraction pipeline 52 is provided with a negative pressure tower top secondary condenser 66 and a vacuum pump 67, the tower bottom of the negative pressure rectifying tower 4 is connected with the pressurizing rectifying tower 21 through a negative pressure tower bottom extraction pipeline 28, the negative pressure tower bottom extraction pipeline 28 is provided with a negative pressure tower bottom pump 29, a pressurizing tower primary feed preheater 19 and a pressurizing tower secondary feed preheater 20, the gas phase at the top of the negative pressure rectifying tower 4 enters the negative pressure tower reflux tank 46 after being condensed, a part of liquid phase in the negative pressure tower reflux tank 46 is refluxed to the negative pressure rectifying tower 4, and the liquid phase is extracted as refined methanol tank 18, and the gas phase in the negative pressure tower reflux tank 46 is condensed by the negative pressure tower top secondary condenser 66 and then subjected to subsequent treatment;
The bottom of the pressurized rectifying tower 21 is connected with the normal pressure rectifying tower 15 through a pressurized tower kettle extraction pipeline 32, a pressurized tower kettle pump 64 is arranged on the pressurized tower kettle extraction pipeline 32, the pressurized tower kettle extraction pipeline 32 passes through the pressurized tower primary feed preheater 19 to provide heat required for heating raw materials for the pressurized tower primary feed preheater 19, miscellaneous alcohol is extracted from the side line of the normal pressure rectifying tower 15, the tower kettle of the normal pressure rectifying tower 15 is provided with a normal pressure tower kettle extraction pipeline 30, the normal pressure tower kettle extraction pipeline 30 is used for extracting waste water, and the normal pressure tower kettle extraction pipeline 30 is provided with a normal pressure tower kettle pump 31.
Preferably, the embodiment fully utilizes the heat of the tops of the pre-rectifying tower 2, the first rectifying tower and the second rectifying tower, the heat of the bottoms of the pre-rectifying tower 2, the first rectifying tower and the second rectifying tower and the waste heat of the steam condensate, and specifically:
The top of the pre-rectifying tower 2 is connected with a negative pressure tower reboiler I3 through a pre-tower top extraction pipeline 39, the output end of the negative pressure tower reboiler I3 is connected with a pre-rectifying tower buffer tank 5 through a negative pressure tower reboiler I output pipeline 40, the bottom of the pre-rectifying tower buffer tank 5 is provided with a pre-tower reflux pipeline 41, the pre-tower reflux pipeline 41 is connected with the upper part of the pre-rectifying tower 2, the pre-rectifying tower reflux pipeline 41 is provided with a pre-tower reflux pump 42, one side of the pre-rectifying tower buffer tank 5 is connected with an extraction water pipeline 43, the upper part of the pre-rectifying tower buffer tank 5 is provided with a gas phase extraction pipeline 6, after the gas phase at the top of the pre-rectifying tower 2 exchanges heat with the negative pressure tower reboiler I3, the gas phase enters the pre-rectifying tower buffer tank 5, the extraction water is introduced into the pre-rectifying tower buffer tank 5, and the liquid phase is extracted through the gas phase extraction pipeline 41, and the gas phase at the top of the pre-rectifying tower 2 is heated against the negative pressure tower reboiler I3, the heat of the pre-rectifying tower 2 is fully utilized, the heat of the pre-rectifying tower 4 is saved, and the circulating water is not required to be cooled by the circulating water again through the water cooling circulation;
The top of the pressurizing rectifying tower 21 is connected with the pre-tower reboiler 22 and the normal pressure tower reboiler 24 through a pressurizing tower gas phase extraction pipeline 57, the output end of the pre-tower reboiler 22 and the output end of the normal pressure tower reboiler 24 are both connected with the pressurizing tower reflux tank 23, a pressurizing tower reflux tank liquid phase extraction pipeline 58 is arranged at the bottom of the pressurizing tower reflux tank 23, the pressurizing tower reflux tank liquid phase extraction pipeline 58 is provided with a pressurizing tower reflux pump 59, the pressurizing tower reflux tank liquid phase extraction pipeline 58 is respectively connected with a pressurizing tower reflux pipeline 60 and a pressurizing tower rectifying methanol extraction pipeline 61, wherein the pressurizing tower reflux pipeline 60 is connected with the middle upper part of the pressurizing rectifying tower 21, the pressurizing tower methanol extraction pipeline 61 is connected with the rectifying methanol tank 18;
The top of the normal pressure rectifying tower 15 is respectively connected with a negative pressure tower reboiler II 16 through a normal pressure tower gas phase extraction pipeline 44, the output end of the negative pressure tower reboiler II 16 is connected with a normal pressure tower reflux tank 17, the bottom of the normal pressure tower reflux tank 17 is provided with a normal pressure tower reflux tank liquid phase extraction pipeline 53, the normal pressure tower reflux tank liquid phase extraction pipeline 53 is provided with a normal pressure tower reflux pump 54, the normal pressure tower reflux tank liquid phase extraction pipeline 53 is respectively connected with a normal pressure tower reflux pipeline 55 and a normal pressure tower rectifying methanol extraction pipeline 56, wherein the normal pressure tower reflux pipeline 55 is connected with the upper part of the normal pressure rectifying tower 15, the normal pressure tower rectifying methanol extraction pipeline 56 is connected with a rectifying methanol tank 18, the gas phase at the top of the normal pressure rectifying tower 15 is respectively provided with a pre-tower reboiler 22 and a negative pressure tower reboiler II, after heat supply, the gas phase enters the normal pressure tower reflux tank 17, and the liquid phase in the normal pressure tower reflux tank 17 is partially refluxed to the rectifying tower 15, and part of the liquid phase in the normal pressure reflux tank 15 is extracted into the rectifying methanol tank 18 as rectifying methanol;
The pressurizing tower reboiler 25 supplies heat through steam, a steam pipeline 62 sequentially passes through the pressurizing tower reboiler 25, the pressurizing tower secondary feed preheater 20 and the pre-tower feed preheater 1, and the output end of the pre-tower feed preheater 1 is connected with a condensate pipeline 63, namely, the pressurizing tower secondary feed preheater 20 adopts the steam condensate of the pressurizing tower reboiler 25 to preheat, and the pre-tower feed preheater 1 adopts the steam condensate of the pressurizing tower secondary feed preheater 20 to preheat, so that the consumption of steam is reduced.
Embodiment III:
the embodiment provides a refining process of crude methanol with high water content, which comprises the following steps:
The crude methanol enters a pre-rectifying tower 2 for rectification after being preheated by a pre-tower feeding preheater 1, wherein the gas phase at the top of the pre-rectifying tower 2 goes to a negative pressure tower reboiler I3 to provide heat required by distillation for a negative pressure rectifying tower 4, then enters a pre-tower buffer tank 5, the liquid phase in the pre-tower buffer tank 5 flows back to the pre-rectifying tower 2, and the gas phase in the pre-tower buffer tank 5 is extracted through a gas phase extraction pipeline 6;
The material in the tower kettle of the pre-rectifying tower 2 enters the dehydration rectifying tower 7, the material in the tower kettle of the pre-rectifying tower 2 enters the dehydration rectifying tower 7 and is preheated by the dehydration tower feed preheater 8, the gas phase in the tower top of the dehydration rectifying tower 7 is pressurized and heated by the compressor 9 and then goes to the dehydration tower reboiler 10 to provide the heat required by distillation for the dehydration rectifying tower 7, then goes to the pre-tower steam reboiler 11 to provide the heat required by distillation for the pre-rectifying tower 2, then enters the dehydration tower reflux tank 13 after being condensed by the dehydration tower top condenser 12, and part of the liquid phase in the dehydration tower reflux tank 13 flows back to the dehydration rectifying tower 7 and the other part enters the negative pressure rectifying tower 4;
a part of gas phase at the top of the negative pressure rectifying tower 4 is refluxed to the negative pressure rectifying tower 4 after being condensed, and the other part of gas phase is taken as refined methanol to be extracted, and the extracted refined methanol is extracted into a refined methanol tank 18;
the first rectifying tower adopts an atmospheric rectifying tower 15, the gas phase at the top of the atmospheric rectifying tower 15 goes to a negative pressure tower reboiler II to provide heat for distillation of a negative pressure rectifying tower 4, then enters an atmospheric tower reflux tank 17, and the liquid phase part of the atmospheric tower reflux tank 17 is refluxed to the atmospheric rectifying tower 15, and part of the liquid phase part is taken as refined methanol to be extracted, and the extracted refined methanol is extracted into a refined methanol tank 18;
The second rectifying tower adopts a pressurizing rectifying tower 21, a part of gas phase at the top of the pressurizing rectifying tower 21 goes to a pre-tower reboiler 22 to provide heat required by distillation for the pre-rectifying tower 2, then enters a pressurizing tower reflux tank 23, the other part of gas phase at the top of the pressurizing rectifying tower 21 goes to an atmospheric tower reboiler 24 to provide heat required by distillation for the atmospheric rectifying tower 15, then enters the pressurizing tower reflux tank 23, a part of liquid phase in the pressurizing tower reflux tank 23 flows back to the pressurizing rectifying tower 21, a part of liquid phase is taken as refined methanol to be taken out, the material at the bottom of the pressurizing rectifying tower 21 goes to a pressurizing tower primary feeding preheater 19 to provide heat required by heating the material for the pressurizing tower primary feeding preheater 19, and then is discharged as waste water.
In this embodiment, the pressurizing tower reboiler 25 supplies heat through steam, the source of the steam may be common boiler steam, or may be steam generated in the reaction section, and the steam may be selected according to specific situations, and is not specifically limited in this embodiment, after the heat is provided by the pressurizing tower reboiler 25, the pressurizing tower secondary feed preheater 20, the atmospheric tower feed preheater 14, and the pre-tower feed preheater 1 in sequence, the steam is extracted as condensate, that is, the pressurizing tower secondary feed preheater 20 is preheated by using the steam condensate of the pressurizing tower reboiler 25, the atmospheric tower feed preheater 14 is preheated by using the steam condensate of the pressurizing tower secondary feed preheater 20, and the pre-tower feed preheater 1 is preheated by using the atmospheric tower feed preheater 14, thereby reducing the consumption of steam.
Embodiment four:
The difference between this embodiment and the third embodiment is that the first rectifying tower is a pressurized rectifying tower 21, and the second rectifying tower is an atmospheric rectifying tower 15;
Specifically:
The crude methanol enters a pre-rectifying tower 2 for rectification after being preheated by a pre-tower feeding and heating device 1, wherein the gas phase at the top of the pre-rectifying tower 2 goes to a negative pressure tower reboiler I3 to provide heat required by distillation for a negative pressure rectifying tower 4, then enters a pre-tower buffer tank 5, the liquid phase in the pre-tower buffer tank 5 flows back to the pre-rectifying tower 2, and the gas phase in the pre-tower buffer tank 5 is extracted through a gas phase extraction pipeline 6;
The material in the tower kettle of the pre-rectifying tower 2 enters the dehydration rectifying tower 7, the material in the tower kettle of the pre-rectifying tower 2 enters the dehydration rectifying tower 7 and is preheated by the dehydration tower feed preheater 8, the gas phase in the tower top of the dehydration rectifying tower 7 is pressurized and heated by the compressor 9 and then goes to the dehydration tower reboiler 10 to provide the heat required by distillation for the dehydration rectifying tower 7, then goes to the pre-tower steam reboiler 11 to provide the heat required by distillation for the pre-rectifying tower 2, then enters the dehydration tower reflux tank 13 after being condensed by the dehydration tower top condenser 12, and part of the liquid phase in the dehydration tower reflux tank 13 flows back to the dehydration rectifying tower 7 and the other part enters the negative pressure rectifying tower 4;
A part of gas phase at the top of the negative pressure rectifying tower 4 is refluxed to the negative pressure rectifying tower 4 after being condensed, and the other part of gas phase is taken as refined methanol to be extracted, and the extracted refined methanol is extracted into a refined methanol tank 18;
The first rectifying tower adopts a pressurized rectifying tower 21, the second rectifying tower adopts a normal pressure rectifying tower 15, a part of gas phase at the top of the pressurized rectifying tower 21 goes to a pre-tower reboiler 22 to provide heat required by distillation for the pre-rectifying tower 2, a part of gas phase goes to a normal pressure tower reboiler 24 to provide heat required by distillation for the normal pressure rectifying tower 15, then enters a pressurized tower reflux tank 23, a part of liquid phase of the pressurized tower reflux tank 23 is refluxed to the pressurized rectifying tower 21, a part of the liquid phase is taken as refined methanol to be extracted, and the extracted refined methanol is extracted into a refined methanol tank 18;
The second rectifying tower adopts an atmospheric rectifying tower 15, the gas phase at the top of the atmospheric rectifying tower 15 goes to a second negative pressure tower reboiler 16 to provide heat for distillation of the negative pressure rectifying tower 4, and then enters an atmospheric tower reflux tank 17, a part of liquid phase in the atmospheric tower reflux tank 17 is refluxed to the atmospheric rectifying tower 15, a part of liquid phase is taken as refined methanol to be extracted, and the extracted refined methanol is taken into a refined methanol tank 18;
In this embodiment, the pressurizing tower reboiler 25 supplies heat through steam, the source of the steam may be common boiler steam, or may be steam generated in the reaction section, and the steam may be selected according to specific conditions, which is not specifically limited in this embodiment, and after the pressurizing tower reboiler 25, the pressurizing tower secondary feed preheater 20 and the pre-tower feed preheater 1 sequentially supply heat, the steam is extracted as condensate, that is, the pressurizing tower secondary feed preheater 20 is preheated by using the steam condensate of the pressurizing tower reboiler 25, and the pre-tower feed preheater 1 is preheated by using the steam condensate of the pressurizing tower secondary feed preheater 20, thereby reducing consumption of steam.
Fifth embodiment:
The embodiment provides specific application occasions of the first embodiment and the third embodiment, namely, the first rectifying tower adopts the normal pressure rectifying tower 15, and the second rectifying tower adopts the pressurized rectifying tower 21;
The raw materials of the crude methanol comprise 65 percent of methanol, 35 to 40 percent of water and 300ppm of ethanol, wherein the raw material temperature is 40 ℃, the raw material pressure is 500KPaG, and the raw material flow is 20000KG/H;
The crude methanol enters a pre-rectifying tower 2 after being preheated, the feeding temperature of the pre-rectifying tower 2 is 74 ℃, the feeding pressure of the pre-rectifying tower 2 is 500KPaG, the tower top temperature of the pre-rectifying tower 2 is 70 ℃, the tower bottom temperature of the pre-rectifying tower 2 is 81 ℃, the tower top pressure and the tower bottom pressure of the pre-rectifying tower 2 are respectively 20 ℃ and 23 ℃, the reflux temperature of the pre-rectifying tower 2 is 62 ℃, the reflux flow rate of the pre-rectifying tower 2 is 1843KG/H, the tower bottom adoption amount of the pre-rectifying tower 2 is 21444KPaG, the extraction water temperature of a pre-rectifying buffer tank 5 is 65 ℃, the extraction water pressure is 193KPaG, the extraction water flow rate is 1500KG/H, and the purge flow rate of the pre-rectifying buffer tank 5 is 31.4KG/H;
the material in the tower kettle of the pre-rectifying tower 2 enters a dehydration rectifying tower 7 after being preheated by a dehydration tower feed preheater 8, the feeding temperature of the dehydration rectifying tower 7 is 81 ℃, the feeding pressure of the dehydration rectifying tower 7 is 500KPaG, the tower top temperature and the tower kettle temperature of the dehydration rectifying tower 7 are respectively 62 ℃ and 96 ℃, the tower top pressure and the tower kettle pressure of the dehydration rectifying tower 7 are respectively-20 KPaG and-15 KPaG, the flow rate of a tower top gas phase inlet compressor 9 of the dehydration rectifying tower 7 is 22600KG/H, the temperature of a tower top gas phase inlet compressor 9 of the dehydration rectifying tower 7 is 204 ℃, the pressure of a tower top gas phase inlet compressor 9 of the dehydration rectifying tower 7 is 230KPaG, the temperature (wastewater temperature) after heat exchange between the tower kettle of the dehydration rectifying tower 7 and the dehydration tower feed preheater 8 is 95 ℃, and the extraction rate of the tower kettle of the dehydration rectifying tower 7 is 7474KG/H;
After the gas phase at the top of the dehydration rectifying tower 7 is compressed and heated by a compressor 9, the gas phase is removed from a dehydration tower reboiler 10 to provide heat required by distillation for the dehydration rectifying tower 7, then part of the gas phase is returned to the dehydration rectifying tower 7 after condensation, part of the gas phase enters a negative pressure rectifying tower 4, the feeding temperature of the negative pressure rectifying tower 4 is 62 ℃, the feeding pressure of the negative pressure rectifying tower 4 is 900KPaG, the feeding flow of the negative pressure rectifying tower 4 is 13970KG/H, the top temperature and the bottom temperature of the negative pressure rectifying tower 4 are 52 ℃ and 57 ℃, the top pressure and the bottom pressure of the negative pressure rectifying tower 4 are-45 KPaG and-40 KPaG respectively, the top extraction amount of the negative pressure rectifying tower 4 is 6460KG/H, the reflux ratio of the negative pressure rectifying tower 4 is 1:3, and the bottom extraction amount of the negative pressure rectifying tower 4 is 7510KG/H;
The material in the tower kettle of the negative pressure rectifying tower 4 is preheated by the feeding preheater 14 of the normal pressure tower, and then enters the normal pressure rectifying tower 15, wherein the feeding temperature of the normal pressure rectifying tower 15 is 57 ℃, the feeding pressure of the normal pressure rectifying tower 15 is 460KPaG, the feeding flow rate of the normal pressure rectifying tower 15 is 7510KG/H, the tower top temperature and the tower kettle temperature of the normal pressure rectifying tower 15 are respectively 72 ℃ and 82 ℃, the tower top pressure and the tower kettle pressure of the normal pressure rectifying tower 15 are respectively 30KPaG and 50KPaG, the tower top extraction amount of the normal pressure rectifying tower 15 is 2950KG/H, the reflux ratio of the normal pressure rectifying tower 15 is 2.3, and the tower kettle extraction amount of the normal pressure rectifying tower 15 is 4560KG/H;
The material in the tower kettle of the normal pressure rectifying tower 15 is preheated by a first-stage feed preheater 19 and a second-stage feed preheater 20 of the pressurizing tower and then enters the pressurizing rectifying tower 21, the feeding temperature of the pressurizing rectifying tower 21 is 132 ℃, the feeding pressure of the pressurizing rectifying tower 21 is 600KPaG, the feeding flow rate of the pressurizing rectifying tower 21 is 4560KG/H, the tower top temperature and the tower kettle temperature of the pressurizing rectifying tower 21 are 120 ℃ and 163 ℃, the tower top pressure and the tower kettle pressure of the pressurizing rectifying tower 21 are 550KPaG and 565KPaG respectively, the tower top extraction amount of the pressurizing rectifying tower 21 is 3010KG/H, the reflux ratio of the pressurizing rectifying tower 21 is 5, the tower kettle extraction amount of the pressurizing rectifying tower 21 is 950KG/H, the side extraction temperature of the pressurizing rectifying tower 21 is 134 ℃, the side extraction pressure of the pressurizing rectifying tower 21 is 563KPaG, and the side extraction flow rate of the pressurizing rectifying tower 21 is 600KG/H;
In the embodiment, the purity of the refined methanol extracted by the negative pressure rectifying tower 4, the purity of the refined methanol extracted by the normal pressure rectifying tower 15 and the purity of the refined methanol extracted by the pressurized rectifying tower 21 can reach 99.99%, the ethanol content is less than or equal to 50ppm after the refined methanol extracted by the negative pressure rectifying tower 4, the refined methanol extracted by the normal pressure rectifying tower 15 and the refined methanol extracted by the pressurized rectifying tower 21 are combined, the methanol content is less than or equal to 10ppm after the wastewater extracted by the pressurized rectifying tower 21 and the wastewater extracted by the dehydration rectifying tower 7 are mixed, the mixture can be directly discharged after reaching the standard, and the consumption of steam in the embodiment is 0.69t steam/t of refined alcohol.
In summary, by adopting the technical scheme, the high-water-content crude methanol can be refined by arranging the dehydration rectifying tower, the energy at the top of the dehydration rectifying tower is fully recycled through the compressor (heat pump) and is used for providing heat for the reboiler of the dehydration rectifying tower, the distillate at the bottom of the dehydration rectifying tower is heated, the materials subjected to heat exchange with the reboiler of the dehydration rectifying tower are not directly extracted and enter the negative pressure rectifying tower, but are treated by the reflux tank of the dehydration rectifying tower, and then partially reflux to the dehydration rectifying tower, and partially enter the negative pressure rectifying tower, so that the accuracy of subsequent distillation is further ensured, and the accuracy of a final methanol product is further ensured; the application can be used for converting the low-grade heat at the top of the dehydration rectifying tower into high-grade heat to meet the heat requirement of a reboiler of the dehydration rectifying tower, and for crude methanol with the water content of 35 percent, the methanol content after dehydration can reach 91 percent, the methanol purity after refining is 99.99 percent, the ethanol content in refined methanol is less than or equal to 50ppm, and the methanol content in waste water is less than or equal to 10ppm, thereby being capable of reaching the standard and being discharged.
In addition, the application has the following advantages:
1. The steam at the top of the pre-rectifying tower supplies heat for the reboiler of the negative pressure tower, provides heat for the distillation of the negative pressure rectifying tower, fully utilizes the heat of the steam at the top of the pre-rectifying tower, saves the steam of the negative pressure rectifying tower, reduces the steam consumption of a system, does not need to adopt circulating water cooling at the top of the pre-rectifying tower, and saves a large amount of circulating water;
2. The method fully utilizes the steam heat of the first rectifying tower and the second rectifying tower, when the first rectifying tower and the rectifying tower adopt an atmospheric rectifying tower and a pressurized rectifying tower respectively, the steam at the top of the atmospheric rectifying tower provides heat for a reboiler II of the negative pressure tower, so as to provide heat required by distillation for the negative pressure rectifying tower, and the heat at the top of the atmospheric rectifying tower is utilized, thereby saving the steam of the negative pressure rectifying tower;
When the first rectifying tower and the rectifying tower respectively adopt a pressurized rectifying tower and an atmospheric rectifying tower, the steam at the top of the pressurized rectifying tower provides heat for a pre-rectifying tower reboiler and an atmospheric rectifying tower reboiler, and further provides heat required by distillation for the pre-rectifying tower and the atmospheric rectifying tower, the heat at the top of the pressurized rectifying tower is utilized, the steam of the pre-rectifying tower and the atmospheric rectifying tower is saved, the steam at the top of the atmospheric rectifying tower provides heat for a negative pressure rectifying tower reboiler II, and further provides heat required by distillation for the negative pressure rectifying tower, the heat at the top of the atmospheric rectifying tower is utilized, and the steam of the negative pressure rectifying tower is saved;
3. When the first rectifying tower and the rectifying tower adopt an atmospheric rectifying tower and a pressurizing rectifying tower respectively, the materials in the kettle of the pressurizing tower provide heat for a first-stage feeding preheater of the pressurizing tower, and steam is adopted as condensate after the heat is provided by a reboiler of the pressurizing tower, a second-stage feeding preheater of the pressurizing tower, a feeding preheater of the atmospheric tower and a feeding preheater of the pre-tower in turn;
When the rectifying tower I and the rectifying tower respectively adopt a pressurized rectifying tower and an atmospheric rectifying tower, the materials in the tower kettle of the pressurized tower are sent to a first-stage feeding preheater of the pressurized tower, heat required for heating the materials is provided for the first-stage feeding preheater of the pressurized tower and then enter the atmospheric tower;
4. The application fully utilizes the heat of the tower top of each tower and the residual heat of the tower kettle condensate and the steam condensate, ensures that the unit steam consumption is less than or equal to 0.7t steam/t refined alcohol while ensuring that the methanol product is more than 99.99 percent, greatly reduces the steam consumption of the system and realizes the multi-stage utilization of energy and the heat coupling;
5. The water content and the alcohol content in the refined methanol obtained by the method can be freely regulated and controlled, and the wastewater can be discharged up to the standard without further treatment.
The above devices, connection relationships, etc. which are not specifically described belong to the prior art, and the present invention is not specifically described herein.
The preferred embodiments of the present application have been described in detail above with reference to the accompanying drawings, but the present application is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present application within the scope of the technical concept of the present application, and all the simple modifications belong to the protection scope of the present application.
In addition, the specific features described in the above embodiments may be combined in any suitable manner, and various possible combinations of the present application are not described separately in order to avoid unnecessary repetition, unless otherwise contradicted.
Moreover, any combination of the various embodiments of the application can be made without departing from the spirit of the application, and the application is also to be regarded as the disclosure of the application.
Claims (10)
1. The utility model provides a high water content crude methanol refining device, its characterized in that, including pre-rectifying column (2), dehydration rectifying column (7), negative pressure rectifying column (4), rectifying column one, rectifying column two that connect gradually, the top of dehydration rectifying column (7) is provided with dehydration tower gas phase extraction pipeline (33), and dehydration tower gas phase extraction pipeline (33) are connected with dehydration tower reboiler (10), be provided with compressor (9) on dehydration tower gas phase extraction pipeline (33), the output of dehydration tower reboiler (10) is connected with dehydration tower reflux drum (13) through dehydration tower reboiler output pipeline (34), be provided with dehydration tower top condenser (12) on dehydration tower reboiler output pipeline (34), the bottom of dehydration tower reflux drum (13) is provided with dehydration tower reflux drum extraction pipeline (35), and dehydration tower reflux drum extraction pipeline (35) are connected with dehydration tower reflux drum (37), negative pressure tower feed line (38) respectively, dehydration tower reflux drum (37) are connected with the upper portion of dehydration rectifying column (7), and negative pressure rectifying column (4) are connected.
2. A high water content crude methanol refining apparatus as claimed in claim 1, wherein the dehydration column reboiler output line (34) passes through a pre-column steam reboiler (11).
3. The high-water-content crude methanol refining device according to claim 1, wherein the top of the pre-rectifying tower (2) is connected with a negative pressure tower reboiler I (3) through a pre-tower top extraction pipeline (39), the output end of the negative pressure tower reboiler I (3) is connected with a pre-tower buffer tank (5) through a negative pressure tower reboiler I output pipeline (40), the bottom of the pre-tower buffer tank (5) is connected with the upper part of the pre-rectifying tower (2) through a pre-tower reflux pipeline (41), one side of the pre-tower buffer tank (5) is provided with an extraction water pipeline (43), and the upper part of the pre-tower buffer tank (5) is provided with a gas phase extraction pipeline (6).
4. The high-water-content crude methanol refining device according to claim 1, wherein the bottom of the pre-rectifying tower (2) is connected with the dehydration rectifying tower (7) through a pre-tower kettle extraction pipeline (26), a pre-tower kettle pump (27) and a dehydration tower feed preheater (8) are arranged on the pre-tower kettle extraction pipeline (26), wastewater is extracted from the tower kettle of the dehydration rectifying tower (7) through a dehydration tower kettle extraction pipeline (65), and the dehydration tower kettle extraction pipeline (65) passes through the dehydration tower feed preheater (8).
5. The high-water-content crude methanol refining device according to claim 1, wherein the first rectifying tower and the rectifying tower adopt an atmospheric rectifying tower (15) and a pressurized rectifying tower (21) respectively, the top of the atmospheric rectifying tower (15) is connected with a negative pressure tower reboiler II (16) through an atmospheric tower gas phase extraction pipeline (44), the output end of the negative pressure tower reboiler II (16) is connected with an atmospheric tower reflux tank (17), an atmospheric tower reflux tank liquid phase extraction pipeline (53) is arranged at the bottom of the atmospheric tower reflux tank (17), the atmospheric tower reflux tank liquid phase extraction pipeline (53) is respectively connected with an atmospheric tower reflux pipeline (55) and an atmospheric tower refined methanol extraction pipeline (56), and the atmospheric tower reflux pipeline (55) is connected with the upper part of the atmospheric rectifying tower (15); the top of the pressurizing rectifying tower (21) is respectively connected with a pre-tower reboiler (22) and an atmospheric tower reboiler (24) through a pressurizing tower gas phase extraction pipeline (57), the output end of the pre-tower reboiler (22) and the output end of the atmospheric tower reboiler (24) are respectively connected with a pressurizing tower reflux tank (23), the bottom of the pressurizing tower reflux tank (23) is provided with a pressurizing tower reflux tank liquid phase extraction pipeline (58), the pressurizing tower reflux tank liquid phase extraction pipeline (58) is respectively connected with a pressurizing tower reflux pipeline (60) and a pressurizing tower refined methanol extraction pipeline (61), the pressure column reflux line (60) is connected to the upper part of the pressure rectifying column (21).
6. The high-water-content crude methanol refining device according to claim 5, wherein a tower kettle of the negative pressure rectifying tower (4) is connected with the normal pressure rectifying tower (15) through a negative pressure tower kettle extraction pipeline (28), the negative pressure tower kettle extraction pipeline (28) is provided with an normal pressure tower feed preheater (14), the bottom of the normal pressure rectifying tower (15) is connected with the pressurizing rectifying tower (21) through a normal pressure tower kettle extraction pipeline (30), a pressurizing tower primary feed preheater (19) and a pressurizing tower secondary feed preheater (20) are arranged on the normal pressure tower kettle extraction pipeline (30), a pressurizing tower kettle extraction pipeline (32) is arranged on a tower kettle of the pressurizing rectifying tower (21), waste water is extracted from the pressurizing tower kettle extraction pipeline (32), and the pressurizing tower kettle extraction pipeline (32) passes through the pressurizing tower primary feed preheater (19).
7. The high water content crude methanol refining apparatus as set forth in claim 6, wherein the steam line (62) passes through the pressurizing tower reboiler (25), the pressurizing tower secondary feed preheater (20), the atmospheric tower feed preheater (14), and the pre-tower feed preheater (1) in this order, and the condensate line (63) is connected to the output end of the pre-tower feed preheater (1).
8. The high-water-content crude methanol refining device as set forth in claim 1, wherein the first rectifying tower and the rectifying tower adopt a pressurizing rectifying tower (21) and an atmospheric rectifying tower (15) respectively, the top of the pressurizing rectifying tower (21) is connected with a pre-tower reboiler (22) and an atmospheric tower reboiler (24) respectively through a pressurizing tower gas phase extraction pipeline (57), the output end of the pre-tower reboiler (22) and the output end of the atmospheric tower reboiler (24) are connected with a pressurizing tower reflux tank (23), the bottom of the pressurizing tower reflux tank (23) is provided with a pressurizing tower reflux tank liquid phase extraction pipeline (58), the pressurizing tower reflux tank liquid phase extraction pipeline (58) is connected with a pressurizing tower reflux pipeline (60) and a pressurizing tower methanol extraction pipeline (61) respectively, the pressurizing tower reflux pipeline (60) is connected with the upper part of the pressurizing rectifying tower (21), the top of the pressurizing rectifying tower (15) is connected with a negative pressure tower (16) through a negative pressure tower gas phase extraction pipeline (44) respectively, the output end of the negative pressure tower reboiler (16) is connected with an atmospheric tower reflux tank (17) and an atmospheric tower reflux tank (53) reflux tank (53) respectively, the reflux pipeline (55) of the normal pressure tower is connected with the upper part of the normal pressure rectifying tower (15).
9. The high-water-content crude methanol refining device according to claim 8, wherein a tower kettle of the negative pressure rectifying tower (4) is connected with the pressurizing rectifying tower (21) through a negative pressure tower kettle extraction pipeline (28), the negative pressure tower kettle extraction pipeline (28) is provided with a pressurizing tower primary feed preheater (19) and a pressurizing tower secondary feed preheater (20), a tower kettle of the pressurizing rectifying tower (21) is provided with a pressurizing tower kettle extraction pipeline (32), the pressurizing tower kettle extraction pipeline (32) is connected with the middle upper part of the normal pressure rectifying tower (15), and the pressurizing tower kettle extraction pipeline (32) passes through the pressurizing tower primary feed preheater (19).
10. The high water content crude methanol refining apparatus as set forth in claim 9, wherein the steam line (62) passes through the pressurizing tower reboiler (25), the pressurizing tower secondary feed preheater (20), the pre-tower feed preheater (1) in this order, and the condensate line (63) is connected to the output end of the pre-tower feed preheater (1).
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