CN220194017U - Crude methanol three-tower three-effect heat pump refining process device - Google Patents
Crude methanol three-tower three-effect heat pump refining process device Download PDFInfo
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Abstract
The application provides a crude methanol three-tower three-effect heat pump refining process device, which comprises a pre-rectifying tower, a negative pressure rectifying tower and a pressurizing rectifying tower which are sequentially connected, wherein the lower parts of the pre-rectifying tower, the negative pressure rectifying tower and the pressurizing rectifying tower are respectively connected with a pre-rectifying tower reboiler, a negative pressure rectifying tower reboiler and a pressurizing rectifying tower reboiler; the gas phase at the top of the pressurized rectifying tower is used for supplying heat to the pre-rectifying tower reboiler, and the gas phase at the top of the negative pressure rectifying tower is used for supplying heat to the negative pressure rectifying tower reboiler; the top of the negative pressure rectifying tower and the top of the pressurizing rectifying tower are used for extracting refined methanol; the three-tower three-effect process comprises three main equipment towers of a pre-rectifying tower, a negative pressure rectifying tower and a pressurizing rectifying tower, wherein the three effects realize one effect through the pressurizing rectifying tower, methanol steam at the top of the tower is thermally coupled with a reboiler of the pre-rectifying tower to realize two effects, and the three effects realize heat matching through a heat pump of the negative pressure rectifying tower; the traditional process can be modified, and the energy consumption is greatly reduced.
Description
Technical Field
The application relates to the technical field of chemical equipment, in particular to a crude methanol three-tower three-effect heat pump refining process device.
Background
Methanol is a chemical basic raw material with wide application, is applied to various fields of fine chemical industry, high polymer, pesticide, medicine, energy source and the like, and has important position in the international chemical market; the crude methanol usually contains light component impurities such as dimethyl ether and the like and heavy component impurities such as ethanol and water and the like, and the refined methanol product meeting the quality requirement can be obtained after various impurities are removed through a rectification process; the energy consumption in the methanol rectification process accounts for 20-30% of the total energy consumption of production, which has great influence on the production cost of the product.
On the premise of national development strategy of carbon emission reduction and carbon peak, enterprises must carry out energy-saving technical transformation, reduce carbon footprint and carbon dioxide emission, the traditional methanol refining process in the chemical industry has the technical characteristics of large yield and high energy consumption, and the process flow, the heat exchange network and the like of the methanol refining process further have larger promotion space; the heat utilization of a reboiler and a tower top condenser of the tower equipment is insufficient in the traditional technology, the temperature is basically reduced in a mode of directly cooling circulating water, and the heat is directly lost and is exchanged into the atmosphere; the traditional methanol rectification process adopts single-tower rectification or double-tower rectification, and has the defects of poor product quality, low methanol recovery rate and huge energy consumption in spite of relatively low equipment investment, and the occurrence of a heat pump technology and a thermal coupling technology brings great improvement prospect for energy conservation and emission reduction in the methanol industry, such as: gradually replaced by a three-tower double-effect rectification and four-tower double-effect rectification process (three towers and a recovery tower) developed by the Germany Lurgi company.
Currently, three-tower double-effect or four-tower double-effect rectification technology is adopted in recent domestic production and methanol rectification device establishment; however, along with the stricter carbon emission index background, new technology is needed to replace the prior art to realize the requirement of lower steam unit consumption of refined methanol products, wherein the multi-effect rectification technology and the heat pump technology have remarkable advantages; the multi-effect rectification technology is characterized in that the whole rectification flow is divided into a plurality of towers with different energy levels, the tower top steam of the tower with higher temperature is used for supplying heat to the reboiler of the tower with lower temperature, and the steam is condensed at the same time; in the multi-effect rectification, the methanol vapor generated by the tower top of the tower with higher temperature exchanges heat for the reboilers of other towers, so that the reboiling heat requirement of the tower bottom of the thermally coupled tower can be met while the condensation of the methanol vapor is realized, the steam consumption can be greatly reduced, and the obvious energy-saving effect is further realized; the heat pump technology is characterized in that uncooled methanol vapor at the top of the tower is compressed into high-grade methanol vapor with higher pressure and higher temperature through a compressor, and then is conveyed to the tower kettle to provide a heat source for a reboiler, and meanwhile, the condensation of the methanol vapor is realized.
The applicant has searched that the closest comparison document is found as follows:
comparative document 1: the technical scheme is provided by a three-tower three-effect crude methanol refining process system with the application number of 201820870873.1, and the system comprises a pre-rectifying tower, a pressurized rectifying tower and a normal pressure rectifying tower, wherein at least two reboilers are arranged at the bottom of the pre-rectifying tower, and a bottom extraction outlet of the pre-rectifying tower is connected with a feed inlet of the pressurized rectifying tower; the top extraction outlet of the pressurized rectifying tower is divided into two branches: one is connected to one reboiler at the bottom of the pre-rectifying tower and is returned to be connected with a reflux tank of the pressurized rectifying tower, and the other is connected to the reboiler at the bottom of the normal pressure rectifying tower and is returned to be connected with the reflux tank of the pressurized rectifying tower; the reflux tank of the pressurized rectifying tower is divided into at least two branches: one is connected with the top reflux of the pressurized rectifying tower, and the other is connected with a product extraction device; the bottom extraction port of the pressurized rectifying tower is connected with the feed inlet of the normal pressure rectifying tower; and the top extraction port of the normal pressure rectifying tower is connected with a product extraction device. The utility model can reduce the energy consumption of the methanol refining system and reduce the equipment investment; in the application, the heat coupling of the pressurizing rectifying tower M2 and the normal pressure rectifying tower M3 is double-effect rectification, and the heat coupling of the pressurizing rectifying tower M2 and the pre-rectifying tower M1 is triple-effect rectification.
Comparison document 2: an improved three-tower three-effect crude methanol refining process system with the application number of 201921144708.9 provides a technical scheme, which comprises a pre-rectifying tower, a first rectifying tower and a second rectifying tower; the first rectifying tower and the second rectifying tower are both pressurizing towers; the top outlet of the first rectifying tower is connected to the reboiler at the bottom of the second rectifying tower and returns to the reflux tank of the first rectifying tower, and the non-condensable gas branch of the reflux tank of the first rectifying tower and the top outlet of the second rectifying tower are parallel and flow to each other and are separated out of one reflux tank which is connected to at least one reboiler at the bottom of the pre-rectifying tower and returns to the second rectifying tower; the utility model can further reduce the energy consumption of the system, reduce the load of the three towers, and avoid the difficult transformation of the traditional three-tower methanol rectification process system; in the application, the secondary utilization of the heat of the tower top of the first pressurizing tower can be realized, the triple-effect heat energy utilization of external steam is formed, the heat energy utilization efficiency is greatly improved, and the energy consumption of the methanol rectifying system is effectively reduced. Compared with the disclosed common three-tower three-effect rectification process (the heat of the bottom reboilers of the normal pressure rectification tower and the pre-rectification tower is provided by the gas phase at the top of the pressurizing rectification tower), the heat energy is fully utilized, the overall load of the first rectification tower is obviously reduced, and the preheating heat supply capacity is improved; in the process, the comprehensive energy consumption of each ton of refined methanol can be reduced to 0.71 ton of steam, and compared with the steam consumption of the disclosed common three-tower three-effect rectification process, the steam consumption is reduced by 24.1 percent by 0.85 to 0.90 ton.
The two comparison documents are three-tower three-effect crude methanol refining process systems, but the two comparison documents do not introduce heat pump technology, so that the method has no economic advantage in areas with high steam price and low electricity price, and the two prior art is different from the concept of the application for realizing three effects.
In summary, the present application provides a new technical solution.
Disclosure of Invention
The application provides a crude methanol three-tower three-effect heat pump refining process device, which comprises a pre-rectifying tower, a negative pressure rectifying tower and a pressurizing rectifying tower which are sequentially connected, wherein the lower parts of the pre-rectifying tower, the negative pressure rectifying tower and the pressurizing rectifying tower are respectively connected with a pre-rectifying tower reboiler, a negative pressure rectifying tower reboiler and a pressurizing rectifying tower reboiler; the gas phase at the top of the pressurized rectifying tower is used for supplying heat to the pre-rectifying tower reboiler, and the gas phase at the top of the negative pressure rectifying tower is used for supplying heat to the negative pressure rectifying tower reboiler; and the tops of the negative pressure rectifying tower and the pressurizing rectifying tower are used for extracting refined methanol.
As a preferable scheme, the top of the pressurized rectifying tower 3 is connected with the pre-rectifying tower reboiler 12 through a pressurized rectifying tower top extraction pipeline 33, the top of the negative pressure rectifying tower 2 is connected with the negative pressure rectifying tower reboiler 13 through a negative pressure rectifying tower top extraction pipeline 24, and the tops of the negative pressure rectifying tower 2 and the pressurized rectifying tower 3 respectively extract refined methanol through the negative pressure rectifying tower top extraction pipeline 24 and the pressurized rectifying tower top extraction pipeline 33.
As a preferable scheme, the top of the pre-rectifying tower is connected with a light component impurity extraction device.
As a preferred scheme, the light component impurity extraction device comprises a pre-rectifying tower top extraction pipeline connected with the top of the pre-rectifying tower, wherein the pre-rectifying tower top extraction pipeline is connected with a condenser, the condenser I is respectively connected with a pre-rectifying tower reflux tank and a condenser II, the condenser II is connected with a gas-liquid separation tank, a purge gas discharge pipeline is arranged at the top of the gas-liquid separation tank, extraction water is introduced into the gas-liquid separation tank, the bottom of the gas-liquid separation tank is connected with the pre-rectifying tower reflux tank, and the pre-rectifying tower reflux tank is connected with the pre-rectifying tower through the pre-rectifying tower reflux pipeline.
As a preferable scheme, the top of the negative pressure rectifying tower is connected with a negative pressure rectifying tower reboiler through a negative pressure rectifying tower top extraction pipeline, a compressor is arranged on the negative pressure rectifying tower top extraction pipeline, and the negative pressure rectifying tower top extraction pipeline is used for extracting refined methanol.
As a preferable scheme, a negative pressure tower reflux tank and a negative pressure tower reflux pump are sequentially arranged at the rear part of the compressor, and a negative pressure rectifying tower reflux pipeline is connected to the negative pressure rectifying tower top extraction pipeline at the rear side of the negative pressure tower reflux pump and is connected with a negative pressure rectifying tower.
As a preferable scheme, the top of the negative pressure tower reflux tank is provided with a vacuumizing pipeline, and the vacuumizing pipeline is sequentially provided with a condenser III and a vacuum pump.
As a preferable scheme, a pressurized rectifying tower top extraction pipeline is arranged at the top of the pressurized rectifying tower, and the pressurized rectifying tower top extraction pipeline passes through the pre-rectifying tower reboiler and is used for extracting refined methanol.
As a preferable scheme, a pressurizing tower reflux tank and a pressurizing tower reflux pump are sequentially arranged on a pressurizing rectifying tower top extraction pipeline at the rear side of the pre-rectifying tower reboiler, the pressurizing rectifying tower top extraction pipeline at the rear side of the pressurizing tower reflux pump is connected with a pressurizing rectifying tower reflux pipeline, and the pressurizing rectifying tower reflux pipeline is connected with the pressurizing rectifying tower.
As a preferred scheme, the feed inlet of the prefractionator is provided with a first preheater and a second preheater.
As a preferable scheme, the top extraction pipeline of the pressurized rectifying tower passes through the first preheater.
As a preferable scheme, the tower bottom of the negative pressure rectifying tower is connected with the inlet of the pressurizing rectifying tower through a pipeline at the bottom of the negative pressure rectifying tower, and a negative pressure tower bottom pump, a preheater III and a preheater IV are sequentially arranged on the pipeline at the bottom of the negative pressure rectifying tower between the negative pressure rectifying tower and the pressurizing rectifying tower.
As a preferable scheme, the pressurizing rectifying tower reboiler is connected with a steam condensate tank through a steam heating pipeline, the steam condensate tank is connected with the pressurizing rectifying tower reboiler, condensate is extracted from the bottom of the steam condensate tank through a condensate extraction pipeline, and the condensate extraction pipeline sequentially passes through a preheater IV and a preheater II.
As a preferable scheme, the pre-rectifying tower reboiler comprises a pre-tower start-up reboiler and a pre-tower thermal coupling reboiler, and the top extraction pipeline of the pressurized rectifying tower is connected with the pre-tower thermal coupling reboiler.
As a preferable scheme, the steam heating pipeline is also connected with a pre-tower start-up reboiler, and the pre-tower start-up reboiler is connected with a pre-tower steam condensate tank through a pre-tower steam condensate pipeline.
As a preferable scheme, one side of the pressurizing rectifying tower is connected with a mixed alcohol extraction device, and the bottom of the pressurizing rectifying tower extracts waste water.
As a preferable scheme, the bottom of the pressurized rectifying tower is used for extracting waste water through a waste water extraction pipeline, and the waste water extraction pipeline passes through the preheater III.
As a preferable scheme, the total tower pressure of the pre-rectifying tower is 110-140kPa, the total tower pressure of the negative pressure rectifying tower is 60-90kPa, and the total tower pressure of the T3 pressurizing tower is 250-350kPa.
The method adopts a three-tower three-effect process, and comprises three main equipment towers of a pre-rectifying tower, a negative pressure rectifying tower and a pressurizing rectifying tower; the three effects realize one effect through the pressurizing rectifying tower, the methanol vapor at the tower top is thermally coupled with the reboiler of the pre-rectifying tower to realize two effects, and the three effects realize heat matching through the heat pump of the negative pressure rectifying tower; through above-mentioned technical scheme, this scheme can reach technical effect as follows:
1. the device can produce methanol with the concentration of more than 99.9 percent, and the ethanol content is controlled to be 100ppm;
2. a three-tower three-effect process flow is adopted, a heat exchange network is optimized, and an energy-saving space is improved;
3. compared with the traditional methanol process, the steam unit consumption can be reduced to 0.39-0.44;
4. the traditional process can be modified, and the energy consumption is greatly reduced; the simultaneous use of the thermal coupling technology and the heat pump technology can be realized, and the process innovation degree is improved.
5. The three-tower three-effect in the application has obvious economic advantages for areas with high steam price and low electricity price because of the introduction of the heat pump, and the steam unit consumption of the application can be obviously reduced compared with that of the comparison file 1 and the comparison file 2.
Drawings
FIG. 1 is a flow diagram of the present application;
FIG. 2 is a schematic illustration of a specific connection of the present application;
1. prefractionating tower 2, negative pressure rectifying tower 3, pressurizing rectifying tower 4, and extraction pipeline of tower kettle of prefractionating tower
5. Pre-tower bottom pump 6, negative pressure rectifying tower bottom pipeline 7 and negative pressure tower bottom pump
8. A third preheater 9, a fourth preheater 10, a waste water extraction pipeline 11, a fusel extraction pipeline 12, a pre-rectifying tower reboiler 13, a negative pressure rectifying tower reboiler 14 and a pressurized rectifying tower reboiler
15. Refined methanol tank 16, pre-rectifying tower top extraction pipeline 17 and condenser I
18. Pre-tower reflux drum 19, condenser two 20, purge gas discharge line
21. Gas-liquid separation tank 22, pre-tower reflux line 23, pre-tower reflux pump
24. Negative pressure rectifying column top extraction pipeline 25, compressor 27 and negative pressure column reflux tank
28. Negative pressure tower reflux pump 29, negative pressure rectifying tower reflux pipeline 30 and vacuumizing pipeline
31. Condenser III 32, vacuum pump 33 and extraction pipeline at top of pressurized rectifying tower
34. Condenser IV 35, pressurized tower reflux drum 36, pressurized tower reflux pump
37. A pressurized rectifying tower reflux pipeline 38, a pre-tower start-up reboiler 39, a pre-tower thermal coupling reboiler 40, a first preheater 41, a second preheater 42, a steam heating pipeline 43, a steam condensate tank 44, a condensate extraction pipeline 45 and a pre-tower steam condensate pipeline.
Detailed Description
The following describes the embodiments of the present utility model 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 utility model.
Embodiment one:
the embodiment provides a crude methanol three-tower three-effect heat pump refining process device, which comprises a pre-rectifying tower 1, a negative pressure rectifying tower 2 and a pressurizing rectifying tower 3 which are sequentially connected, wherein the bottom of the pre-rectifying tower 1 is connected with an input port of the negative pressure rectifying tower 2 through a pre-rectifying tower kettle extraction pipeline 4, the pre-rectifying tower kettle extraction pipeline 4 is provided with a pre-rectifying tower kettle pump 5, the pre-rectifying tower kettle pump 5 adopts a conveying pump in the prior art, the specific model is not limited, a technician can select according to specific conditions, the tower kettle of the negative pressure rectifying tower 2 is connected with an inlet of the pressurizing rectifying tower 3 through a negative pressure rectifying tower bottom pipeline 6, a negative pressure tower kettle pump 7, a preheater three 8 and a preheater four 9 are sequentially arranged on the negative pressure rectifying tower bottom pipeline 6 between the negative pressure rectifying tower 2 and the pressurizing rectifying tower 3, wastewater can be extracted through a wastewater extraction device and the bottom of the pressurizing rectifying tower 3, more specifically, the bottom of the pressurizing rectifying tower 3 is connected with a wastewater extraction pipeline 10 through the wastewater extraction pipeline three 8; a mixed alcohol extraction pipeline 11 is arranged at one side of the pressurized rectifying tower 3 and is used for extracting mixed alcohol; the lower parts of the pre-rectifying tower 1, the negative pressure rectifying tower 2 and the pressurizing rectifying tower 3 are respectively connected with a pre-rectifying tower reboiler 12, a negative pressure rectifying tower reboiler 13 and a pressurizing rectifying tower reboiler 14; the top of the pressurized rectifying tower 3 is connected with the pre-rectifying tower reboiler 12 through a pressurized rectifying tower top extraction pipeline 33, a gas phase at the top of the pressurized rectifying tower 3 is used for supplying heat to the pre-rectifying tower reboiler 12, the top of the negative pressure rectifying tower 2 is connected with the negative pressure rectifying tower reboiler 13 through a negative pressure rectifying tower top extraction pipeline 24, and a gas phase at the top of the negative pressure rectifying tower 2 is used for supplying heat to the negative pressure rectifying tower reboiler 13; and the tops of the negative pressure rectifying tower 2 and the pressurized rectifying tower 3 respectively extract refined methanol through a negative pressure rectifying tower top extraction pipeline 24 and a pressurized rectifying tower top extraction pipeline 33, and the refined methanol is preferably stored through a refined methanol tank 15, and the refined methanol tank 15 is used for collecting the extracted refined methanol; and the discharge of the tower bottom of the pressurizing rectifying tower 3 is preheated by a preheater III 8 to feed and convey the preheated material to the wastewater treatment process, and the mixed alcohol is extracted from the side line of the pressurizing rectifying tower 3 to the next treatment process.
The top of the pre-rectifying tower 1 is connected with a light component impurity extraction device, the top of the pre-rectifying tower 1 extracts light component impurities, specifically, the light component impurity extraction device comprises a pre-rectifying tower top extraction pipeline 16 connected with the top of the pre-rectifying tower 1, the pre-rectifying tower top extraction pipeline 16 is connected with a first condenser 17, the first condenser 17 is respectively connected with a pre-rectifying tower reflux tank 18 and a second condenser 19 through pipelines, the second condenser 19 is connected with a gas-liquid separation tank 21 through pipelines, and the top of the gas-liquid separation tank 21 is provided with a purge gas discharge pipeline 20 and a purge gas discharge pipeline 20 for discharging purge gas; the extraction water is introduced into a gas-liquid separation tank 21, the bottom of the gas-liquid separation tank 21 is connected with a pre-tower reflux tank 18, the pre-tower reflux tank 18 is connected with the middle upper part of a pre-rectifying tower 1 through a pre-tower reflux pipeline 22, and a pre-tower reflux pump 23 is arranged on the pre-tower reflux pipeline 22; the light component impurity extraction device extracts light phase components, and part of liquid is refluxed through the gas-liquid separation tank 21 and the pre-tower reflux tank 18, so that methanol carried in the light phase is further recovered, and the methanol recovery rate of the system is improved.
As a preferable scheme, the total tower pressure of the pre-rectifying tower 1 is 110-140kPa, the total tower pressure of the negative pressure rectifying tower 2 is 60-90kPa, and the total tower pressure of the pressurized rectifying tower 3 is 250-350kPa.
Embodiment two:
the present embodiment specifically defines a structure in which a gas phase at the top of the negative pressure rectifying column 2 is used for supplying heat to the negative pressure rectifying column reboiler 13, specifically:
the top of the negative pressure rectifying tower 2 is connected with a negative pressure rectifying tower reboiler 13 through a negative pressure rectifying tower top extraction pipeline 24, a compressor 25 is arranged on the negative pressure rectifying tower top extraction pipeline 24, and the negative pressure rectifying tower reboiler 13 extracts refined methanol through the negative pressure rectifying tower top extraction pipeline 24, namely the negative pressure rectifying tower top extraction pipeline 24 is connected with a refined methanol tank 15; more specifically: a negative pressure tower reflux tank 27 and a negative pressure tower reflux pump 28 are sequentially arranged on the negative pressure rectifying tower top extraction pipeline 24, a negative pressure rectifying tower reflux pipeline 29 is arranged on the negative pressure rectifying tower top extraction pipeline 24 at the rear side of the negative pressure tower reflux pump 28, and the negative pressure rectifying tower reflux pipeline 29 is connected with the negative pressure rectifying tower 2; preferably, a vacuum pipeline 30 is arranged at the top of the negative pressure tower reflux drum 27, and a condenser III 31 and a vacuum pump 32 are sequentially arranged on the vacuum pipeline 30 and used for adjusting the pressure of the negative pressure rectifying tower 2.
The discharged material of the tower bottom of the pre-rectifying tower 1 is conveyed to the negative pressure rectifying tower 2 through the pre-rectifying tower bottom pump 5 for rectifying methanol, the refined methanol vapor produced from the tower top of the negative pressure rectifying tower 2 is conveyed to the negative pressure rectifying tower reboiler 13 for heat exchange and condensation after being compressed through the compressor 25, and is then produced to the negative pressure tower reflux tank 27, a part of the refined methanol vapor is refluxed to the negative pressure rectifying tower 2 through the negative pressure tower reflux pump 28 and the negative pressure rectifying tower reflux pipeline 29, and a part of the refined methanol vapor is conveyed to the refined methanol tank 15; and the discharge of the tower bottom of the negative pressure rectifying tower 2 is preheated by a negative pressure tower bottom pump 7, a third preheater 8 and a fourth preheater 9 and then is conveyed to the pressurizing rectifying tower 3.
Embodiment III:
the present embodiment specifically defines the structure of the gas phase at the top of the pressurized rectifying column 3 for supplying heat to the pre-rectifying column reboiler 12, specifically:
the top of the pressurized rectifying tower 3 is connected with the pre-rectifying tower reboiler 12 through a pressurized rectifying tower top extraction pipeline 33, and the pre-rectifying tower reboiler 12 extracts refined methanol through the pressurized rectifying tower extraction pipeline 33, namely the pre-rectifying tower reboiler 12 is connected with the refined methanol tank 15 through the pressurized rectifying tower extraction pipeline 33; the fourth condenser 34 is arranged on the pressurized rectifying tower extraction pipeline 33, and is preferably arranged at the tail end of the pressurized rectifying tower extraction pipeline 33; the pressurizing rectifying tower extraction pipeline 33 is sequentially provided with a pressurizing tower reflux tank 35 and a pressurizing tower reflux pump 36, the pressurizing rectifying tower overhead extraction pipeline 33 at the rear side of the pressurizing tower reflux pump 36 is connected with a pressurizing rectifying tower reflux pipeline 37, and the pressurizing rectifying tower reflux pipeline 37 is connected with the pressurizing rectifying tower 3; more preferably, the pre-rectifying tower reboiler 12 comprises a pre-rectifying tower start-up reboiler 38 and a pre-rectifying tower thermal coupling reboiler 39, the pressure rectifying tower top extraction line 33 is connected with the pre-rectifying tower thermal coupling reboiler 39, namely, the gas phase at the top of the pressure rectifying tower 3 is used for supplying heat to the pre-rectifying tower thermal coupling reboiler 39, more particularly, the top of the pressure rectifying tower 3 is connected with the pre-rectifying tower thermal coupling reboiler 39 through the pressure rectifying tower top extraction line 33, the pre-rectifying tower thermal coupling reboiler 39 extracts refined methanol through the pressure rectifying tower extraction line 33, namely, the pre-rectifying tower thermal coupling reboiler 39 is connected with the refined methanol tank 15 through the pressure rectifying tower extraction line 33; refined methanol extracted from the top of the pressurized rectifying tower 3 is conveyed to a pre-tower thermal coupling reboiler 39 for heat exchange, the heat exchanged material is conveyed to a pressurized tower reflux tank 35, part of the material is refluxed to the pressurized rectifying tower 3 through a pressurized rectifying tower reflux pipeline 37 by a pressurized tower reflux pump 36, and the other part of the material is conveyed to a refined methanol tank 15 for refined methanol recovery.
Preferably, the feed inlet of the pre-rectifying tower 1 is provided with a first preheater 40 and a second preheater 41, the material of the pre-rectifying tower top extraction pipeline 33 after heat exchange by the pre-tower thermal coupling reboiler 39 is conveyed to the pressurizing tower reflux tank 35, part of the material flows back to the pressurizing rectifying tower 3 through the pressurizing tower reflux pump 36 through the pressurizing rectifying tower reflux pipeline 37, and the other part of the material is extracted from refined methanol to the refined methanol tank 15 after heat exchange by the first preheater 40.
Embodiment four:
the pressurized rectifying column reboiler 14 in this embodiment supplies heat by steam, specifically:
the pressurizing rectifying tower reboiler 14 is connected with a steam heating device and the like through a steam heating pipeline 42, the steam heating pipeline 42 is also connected with a steam condensate tank 43, condensate in the steam heating pipeline 42 is discharged, the steam condensate tank 43 is connected with the pressurizing rectifying tower reboiler 14, the pressurizing rectifying tower reboiler 14 is also connected with the steam heating pipeline 42, condensate is extracted from the bottom of the steam condensate tank 43 through a condensate extraction pipeline 44, and the condensate extraction pipeline 44 sequentially passes through a preheater IV 9 and a preheater II 41; the steam enters the pressurizing rectifying tower reboiler 14 through a steam heating pipeline 42 to exchange heat; the steam condensate after heat exchange by the pressurizing rectifying tower reboiler 14 enters a steam condensate tank 43, and the condensate in the steam condensate tank 43 exchanges heat with the preheater IV 9 and the preheater I41.
Preferably, in order to further improve the steam utilization rate, the steam heating pipeline 42 is further connected to the pre-tower start-up reboiler 38 through a pipeline, the pre-tower start-up reboiler 38 is connected to the steam condensate tank 43 through a pre-tower steam condensate pipeline 45, and the steam condensate after heat exchange of the pre-tower start-up reboiler 38 enters the steam condensate tank 43.
Fifth embodiment:
the embodiment provides a specific application occasion:
when the feeding amount is 27700kg/h and the related parameters of the process are optimized to be optimal, the three-tower three-effect thermal coupling production device is used for producing steam/refined methanol with the energy consumption of about 0.40 ton, wherein the purity of the methanol can reach more than 99.9%, and the ethanol content is less than 100ppm.
By the recovery device, the steam unit consumption in the methanol production process can be greatly reduced, and compared with the steam unit consumption (unit consumption is 1.1-1.5) of the conventional three-tower four-tower process methanol, the energy consumption is reduced to more than one third of that of the conventional process, and the recovery device has good development prospect for energy conservation, emission reduction, yield increase and cost reduction of enterprises.
The working principle of the application is as follows: raw materials are preheated to 70-80 ℃ by a first preheater 40 and a second preheater 41 and are conveyed to a pre-rectifying tower 1, light phase components at the top of the pre-rectifying tower 1 are extracted, a tower bottom discharge of the pre-rectifying tower 1 is conveyed to a negative pressure rectifying tower 2 by a pre-tower bottom pump 5 for rectifying methanol, the rectified methanol vapor extracted at the top of the negative pressure rectifying tower 2 is compressed by a compressor 25 and is conveyed to a negative pressure rectifying tower reboiler 13 for heat exchange and condensation and is extracted to a negative pressure tower reflux tank 27, a part of the rectified methanol is refluxed to the negative pressure rectifying tower 2 by a negative pressure tower reflux pump 28 and a negative pressure rectifying tower reflux pipeline 29, and a part of the rectified methanol is extracted; the discharged material of the tower bottom of the negative pressure rectifying tower 2 is preheated by a negative pressure tower bottom pump 7, a preheater III 8 and a preheater IV 9 and then is conveyed to the pressurizing rectifying tower 3, refined methanol extracted from the tower top of the pressurizing rectifying tower 3 is conveyed to a pre-tower thermal coupling reboiler 39 for heat exchange, the material after heat exchange is conveyed to a pressurizing tower reflux tank 35, a part of the material is refluxed to the pressurizing rectifying tower 3 by a pressurizing tower reflux pump 36 and a pressurizing rectifying tower reflux pipeline 37, and a part of the material extracted refined methanol; and the discharge of the tower bottom of the pressurized rectifying tower 3 is preheated by a preheater III 8 to feed and convey the preheated material to the wastewater treatment process, and the mixed alcohol is extracted from the side line of the pressurized rectifying tower 3 to the next treatment process.
Compared with the conventional methanol refining process, the three-tower three-effect process has obvious energy-saving improvement; comprises three main equipment towers, namely a pre-rectifying tower 1, a negative pressure rectifying tower 2 and a pressurizing rectifying tower 3; the three effects realize one effect through the self pressurizing rectifying tower 3, the methanol vapor at the top of the tower is thermally coupled with the pre-tower thermal coupling reboiler 39 to realize two effects, and the three effects realize heat matching through the self heat pump of the negative pressure rectifying tower 2; the unit consumption of the methanol production steam can be remarkably reduced to 0.39-0.44 (the unit consumption is the unit consumption after the conversion, and the electricity price is 0.3 yuan/degree calculated according to 200 yuan/ton of steam), compared with other conventional processes, the steam consumption is only about one third of that of the conventional processes, the production cost can be greatly reduced for enterprises under the background that the conventional steam is more expensive, and the benefit is more obvious along with the time.
Through above-mentioned technical scheme, this scheme can reach technical effect as follows:
1. the device can produce methanol with the concentration of more than 99.9 percent, and the ethanol content is controlled to be 100ppm;
2. a three-tower three-effect process flow is adopted, a heat exchange network is optimized, and an energy-saving space is improved;
3. compared with the traditional methanol process, the steam unit consumption can be reduced to 0.39-0.44;
4. the traditional process can be modified, and the energy consumption is greatly reduced; the simultaneous use of the thermal coupling technology and the heat pump technology can be realized, and the process innovation degree is improved;
5. the three-tower three-effect in the application has obvious economic advantages for areas with high steam price and low electricity price because of the introduction of the heat pump, and the steam unit consumption of the application can be obviously reduced compared with that of the comparison file 1 and the comparison file 2.
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 foregoing embodiments, and various simple modifications may be made to the technical solutions 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 foregoing embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various possible combinations of the present utility model are not described in detail.
Moreover, any combination of the various embodiments of the present application may be made without departing from the spirit of the present application, which is also to be considered as disclosed herein.
Claims (10)
1. The refining process device of the crude methanol three-tower three-effect heat pump is characterized by comprising a pre-rectifying tower (1), a negative pressure rectifying tower (2) and a pressurizing rectifying tower (3) which are connected in sequence, wherein the lower parts of the pre-rectifying tower (1), the negative pressure rectifying tower (2) and the pressurizing rectifying tower (3) are respectively connected with a pre-rectifying tower reboiler (12), a negative pressure rectifying tower reboiler (13) and a pressurizing rectifying tower reboiler (14); the gas phase at the top of the pressurizing rectifying tower (3) is used for supplying heat to the pre-rectifying tower reboiler (12), and the gas phase at the top of the negative pressure rectifying tower (2) is used for supplying heat to the negative pressure rectifying tower reboiler (13); refined methanol is extracted from the tops of the negative pressure rectifying tower (2) and the pressurizing rectifying tower (3).
2. The crude methanol three-tower three-effect heat pump refining process device according to claim 1, wherein the top of the pre-rectifying tower (1) is connected with a light component impurity extraction device.
3. The crude methanol three-tower three-effect heat pump refining process device according to claim 1, wherein the tower top of the negative pressure rectifying tower (2) is connected with a negative pressure rectifying tower reboiler (13) through a negative pressure rectifying tower top extraction pipeline (24), a compressor (25) is arranged on the negative pressure rectifying tower top extraction pipeline (24), a negative pressure rectifying tower reflux tank (27) and a negative pressure rectifying tower reflux pump (28) are sequentially arranged on the rear side of the compressor (25) of the negative pressure rectifying tower top extraction pipeline (24), a negative pressure rectifying tower reflux pipeline (29) is connected on the negative pressure rectifying tower top extraction pipeline (24) on the rear side of the negative pressure rectifying pump (28), and the negative pressure rectifying tower reflux pipeline (29) is connected with the negative pressure rectifying tower (2); and a negative pressure rectifying tower top extraction pipeline (24) is used for extracting refined methanol.
4. The crude methanol three-tower three-effect heat pump refining process device according to claim 1, wherein a pressurizing rectifying tower top extraction pipeline (33) is arranged at the top of the pressurizing rectifying tower (3), the pressurizing rectifying tower top extraction pipeline (33) passes through the pre-rectifying tower reboiler (12), a pressurizing tower reflux tank (35) and a pressurizing tower reflux pump (36) are sequentially arranged on the pressurizing rectifying tower top extraction pipeline (33) at the rear side of the pre-rectifying tower reboiler (12), the pressurizing rectifying tower top extraction pipeline (33) at the rear side of the pressurizing tower reflux pump (36) is connected with a pressurizing rectifying tower reflux pipeline (37), and the pressurizing rectifying tower reflux pipeline (37) is connected with the pressurizing rectifying tower (3); the top extraction pipeline (33) of the pressurized rectifying tower is used for extracting refined methanol.
5. The three-tower three-effect heat pump refining process device for crude methanol according to claim 4, wherein the feed inlet of the pre-rectifying tower (1) is provided with a first preheater (40) and a second preheater (41).
6. The crude methanol three-tower three-effect heat pump refining process apparatus as set forth in claim 5, wherein the pressurized rectifying tower overhead extraction line (33) passes through a first preheater (40).
7. The crude methanol three-tower three-effect heat pump refining process device according to claim 5, wherein the tower kettle of the negative pressure rectifying tower (2) is connected with the inlet of the pressurizing rectifying tower (3) through a negative pressure rectifying tower bottom pipeline (6), and a negative pressure tower kettle pump (7), a preheater III (8) and a preheater IV (9) are sequentially arranged on the negative pressure rectifying tower bottom pipeline (6) between the negative pressure rectifying tower (2) and the pressurizing rectifying tower (3).
8. The crude methanol three-tower three-effect heat pump refining process device according to claim 7, wherein the pressurizing rectifying tower reboiler (14) supplies heat through a steam heating pipeline (42), the steam heating pipeline (42) is further connected with a steam condensate tank (43), the steam condensate tank (43) is connected with the pressurizing rectifying tower reboiler (14), condensate is extracted from the bottom of the steam condensate tank (43) through a condensate extraction pipeline (44), and the condensate extraction pipeline (44) sequentially passes through a fourth preheater (9) and a second preheater (41).
9. The crude methanol three-tower three-effect heat pump refining process device according to claim 8, wherein the pre-rectifying tower reboiler (12) comprises a pre-tower start-up reboiler (38) and a pre-tower thermal coupling reboiler (39), and the pressurized rectifying tower top extraction pipeline (33) is connected with the pre-tower thermal coupling reboiler (39).
10. The crude methanol three-tower three-effect heat pump refining process device according to claim 9, wherein the steam heating pipeline (42) is further connected with a pre-tower start-up reboiler (38), and the pre-tower start-up reboiler (38) is connected with a steam condensate tank (43) through a pre-tower steam condensate pipeline (45).
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| CN202321742454.7U CN220194017U (en) | 2023-07-04 | 2023-07-04 | Crude methanol three-tower three-effect heat pump refining process device |
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| CN202321742454.7U CN220194017U (en) | 2023-07-04 | 2023-07-04 | Crude methanol three-tower three-effect heat pump refining process device |
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