CN217511198U - Four-tower heat pump thermal coupling methanol rectification device - Google Patents
Four-tower heat pump thermal coupling methanol rectification device Download PDFInfo
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Abstract
The application provides a four-tower heat pump thermal coupling methanol rectification device, which comprises a pre-rectification tower, a negative pressure rectification tower, a pressurizing rectification tower and a fusel recovery tower which are connected in sequence, wherein the adopted total process route is the sequence of the pre-rectification tower, the negative pressure rectification tower, the pressurizing rectification tower and the fusel recovery tower, the methanol is purified, the thermal coupling is fully carried out by combining the waste heat evaporation of waste water and the recycling of condensed water, and the energy-saving advantage of the heat pump technology is exerted, so that the pressure and the difficulty of a waste water treatment section are reduced while the methanol is purified, the average steam consumption of each ton of refined methanol is lower than the lowest steam consumption level of the industry, the energy consumption is saved, the energy waste is reduced, the requirement of the national double-carbon energy-saving policy is responded, and the energy conservation is realized to the greatest extent; the comprehensive steam unit consumption of each ton of refined methanol of the device is 0.25-0.36 ton, the average steam consumption of each ton of refined methanol is 0.81-1.15 ton at present, and the average steam consumption of each ton of refined methanol is lower than the lowest steam consumption level of the industry through the arrangement of the device.
Description
Technical Field
The application relates to the technical field of chemical engineering and coal chemical engineering, in particular to a four-tower heat pump thermal coupling methanol rectification device.
Background
Methanol is an important basic organic chemical raw material and novel energy fuel, the industrial synthesis of methanol almost completely adopts a carbon monoxide pressurized catalytic hydrogenation method, the process comprises the working procedures of gas making, synthesis and purification, methanol synthesis, crude methanol rectification and the like, and the methanol rectification mainly aims at removing volatile components such as dimethyl ether, and ethanol, higher alcohol and water which are difficult to volatilize so as to produce refined methanol meeting the product requirements; with the vigorous development of the coal chemical industry, the scale of the methanol rectification device is larger and larger, how to reduce the energy consumption of a single ton of refined methanol of the methanol refining device becomes the key for the survival of enterprises and the improvement of competitiveness, and the research objects are taken as the key for carrying out deep research by vast researchers and engineering technicians.
The currently widely adopted three-tower methanol rectification (concurrent double-effect rectification) process is that crude methanol is rectified and separated sequentially through a pre-rectification tower, a pressurized rectification tower and a normal-pressure rectification tower, and methanol products are respectively obtained by discharging from the top of the pressurized tower and discharging from the top of the normal-pressure tower; the separation sequence is that a pre-rectifying tower removes light components in the crude methanol, the prognostic crude methanol at the tower bottom enters a pressurized rectifying tower, the condensation latent heat of methanol steam at the top of the pressurized tower is used as a reboiling heat source of an atmospheric tower to realize forward flow double-effect rectification, the fusel is extracted from the side line of the atmospheric tower, and the waste water is discharged from the bottom of the atmospheric tower. The method is a common crude methanol refining process, the energy consumption of the methanol rectification process is about 2417-3223.7 MJ/ton of refined methanol product, the production energy consumption is higher, the total energy consumption is also obviously increased along with the expansion of the methanol refining scale, and the energy-saving process becomes a preferential object of the industry under the background of 'double carbon'.
For the existing device, in order to reduce the energy consumption of the methanol rectification, various attempted solutions are provided at present, for example, a high-pressure tower is additionally arranged and coupled with the existing pressurized tower to form a five-tower triple-effect rectification process, or a heat pump technology is adopted; the five-tower rectification transformation mode directly causes site restrictive factors, tower investment increase, insufficient safety spacing and other problems; the single heat pump rectification also has the engineering problems of increased investment on power equipment and expansion of power utilization distribution stations; the current three-tower triple-effect technology and the improved three-tower triple-effect technology have the advantages that for production expansion type energy conservation, manufacturers with small tower diameters are difficult to meet the production expansion and energy conservation requirements, in addition, under the negative pressure working condition, the separation difficulty of methanol and water and the separation difficulty of methanol and ethanol are reduced, the energy consumption can be obviously reduced, and therefore the technology has engineering advantages.
In summary, in the prior art, the methanol distillation system mainly employs multi-effect distillation, such as five-tower three-effect, five-tower four-effect, three-tower three-effect, improved three-tower three-effect, four-tower four-effect, in individual cases, the scheme that the heat pump is nested into a certain link is also adopted, the average energy consumption of each ton of refined methanol is 0.6-0.9 ton of steam, in the article of 'Heat Pump coupling methanol Multi-effect rectification energy-saving New Process', Wang Dongliang, through the coupling of a heat pump and multiple effects, the energy consumption is further reduced, the energy consumption is reduced to 0.45-0.50 ton of steam/ton of refined methanol, each improved technical innovation obtains the obvious reduction of the energy consumption, based on the background of global climate change, a double-carbon policy gradually falls to the ground, the price of energy is continuously increased, and a better energy-saving process and means are gradually applied; the application aims at combining four towers with a heat pump and multi-effect coupling to form a new technical scheme.
SUMMERY OF THE UTILITY MODEL
The application provides a four-tower heat pump thermal coupling methanol rectification device, including pre-rectifying tower, negative pressure rectifying tower, pressurization rectifying tower, the miscellaneous mellow wine recovery tower that connects gradually, the bottom of negative pressure rectifying tower is connected with negative pressure rectifying tower reboiler one, negative pressure rectifying tower reboiler two, the top of negative pressure rectifying tower through heat exchange pipeline five with negative pressure rectifying tower reboiler two is connected, be equipped with compressor one on the heat exchange pipeline five.
Preferably, the first compressor is at least two parallel compressor sets, and each compressor set at least comprises one compressor.
As a preferred scheme, the bottom of the fusel recovery tower is connected with a first reboiler and a second reboiler of the fusel recovery tower, the first reboiler of the fusel recovery tower is connected with a vertical buffer tank of the fusel, the vertical buffer tank of the fusel is connected with the top of the fusel recovery tower through a third heat exchange pipeline and a top pipeline of the fusel tower, the third heat exchange pipeline is provided with a second compressor, the vertical buffer tank of the fusel is further connected with a methanol gas treatment device through a fourth heat exchange pipeline, and the fourth heat exchange pipeline is provided with a crude methanol circulating pump.
Preferably, the second compressor is at least two parallel compressor sets, and each compressor set at least comprises one compressor.
Preferably, a pre-rectifying tower gas treatment device is connected to the top of the pre-rectifying tower, a pre-rectifying tower reboiler I and a pre-rectifying tower reboiler II are arranged at the lower part of the pre-rectifying tower, and the pre-rectifying tower reboiler I is connected with a pressurized rectifying tower pipeline I at the top of the pressurized rectifying tower through a heat exchange pipeline seven; the two-way of the negative pressure rectifying tower reboiler is connected with a negative pressure rectifying tower liquid treatment device through a heat exchange pipeline six, the top of the pressurized rectifying tower is provided with a pressurized rectifying tower gas treatment device, the pressurized rectifying tower gas treatment device is connected with a rectifying methanol tank area, and the rectifying methanol tank area is also connected with the negative pressure rectifying tower liquid treatment device; and a pressurized rectifying tower reboiler is also arranged at the lower part of the pressurized rectifying tower.
As a preferred scheme, the methanol gas treatment device comprises a first fusel cooler connected with a third heat exchange pipeline and a top pipeline of a fusel tower, the first fusel cooler is connected with a first fusel water recovery tower reflux tank through a first fusel recovery tower pipeline, the first fusel recovery tower pipeline is connected with a fourth heat exchange pipeline, the first fusel water recovery tower reflux tank is connected with a first refined methanol cooler, the second fusel water recovery tower reflux tank is further connected with a second refined methanol cooler through a second fusel recovery tower pipeline, a fusel reflux pump is arranged on the second fusel recovery tower pipeline, and the second fusel recovery tower pipeline is connected with the upper part of a fusel recovery tower through a third fusel recovery tower pipeline.
As a preferable scheme, the bottom of the pressurized rectifying tower and the bottom of the fusel recovery tower are connected with a wastewater treatment device.
As a preferred scheme, the wastewater treatment device comprises a wastewater evaporator connected with an extraction pipeline, the wastewater evaporator is connected with the bottom of the pressurized rectifying tower through a wastewater pipeline, a wastewater pump is arranged on the wastewater pipeline, the top of the wastewater evaporator is connected with a water outlet pipeline, a condensation cooler is arranged on the water outlet pipeline, a water outlet pipeline I is arranged at the bottom of the wastewater evaporator, the wastewater evaporator is further connected with a heater, the heater is connected with the top of the pre-rectifying tower through a heat exchange pipeline I, and the heater is connected with the gas treatment device of the pre-rectifying tower through a heat exchange pipeline II.
Preferably, the waste water pipeline is connected with a first waste water pipeline, and a waste water cooler is arranged on the first waste water pipeline.
Preferably, the water outlet pipeline is further connected with a condensed water reflux pipeline, and the condensed water reflux pipeline is connected with a pre-rectifying tower gas treatment device connected with the top of the pre-rectifying tower.
Preferably, the public bus of the plurality of parallel compressors I is connected with the negative pressure rectifying tower liquid treatment device through a pipeline.
As a preferable scheme, the pre-rectifying tower gas treatment device comprises a first pre-rectifying tower condenser, the first pre-rectifying tower condenser is connected with a second pre-rectifying tower condenser through a first pre-rectifying tower pipeline, the second pre-rectifying tower condenser is connected with a pre-gas-liquid separator through a second pre-rectifying tower pipeline, the pre-gas-liquid separator is connected with a pre-reflux tank through a third pre-rectifying tower pipeline, the pre-reflux tank is connected with the top of the pre-rectifying tower through a reflux pipeline of the pre-rectifying tower, and a pre-rectifying tower reflux pump is arranged on the reflux pipeline of the pre-rectifying tower; the top of the pre-reflux groove is connected with a first condenser of the pre-rectifying tower through a pre-rectifying tower pipeline IV; the pre-reflux tank is connected with the water outlet pipeline through a condensed water reflux pipeline.
As a preferred scheme, the negative pressure rectifying tower liquid treatment device comprises a negative pressure reflux tank connected with a heat exchange pipeline six, the negative pressure reflux tank is connected with the upper part of the negative pressure rectifying tower through a negative pressure distillation tower pipeline I and a negative pressure distillation tower pipeline II, the negative pressure reflux tank is connected with a refined methanol tank area through a negative pressure distillation tower pipeline I and a negative pressure distillation tower pipeline III, and a negative pressure tower first cooler and a negative pressure tower second cooler are sequentially arranged on the negative pressure distillation tower pipeline III between the negative pressure reflux tank and the refined methanol tank area; the second negative pressure distillation tower pipeline and the third negative pressure distillation tower pipeline are both provided with a negative pressure reflux pump; the negative pressure backflow tank is connected with the public end bus through the pipeline, a first pipeline is connected to the negative pressure backflow tank, the first pipeline is connected with a vacuum system, and a condenser is arranged on the first pipeline.
Preferably, the pressurized rectifying tower gas treatment device comprises a pressurized tower cooler, the pressurized tower cooler is connected with the top of the pressurized rectifying tower through a first pressurized rectifying tower pipeline, the pressurized tower cooler is connected with the rectifying methanol tank area through a second pressurized rectifying tower pipeline, a pressurized tower reflux tank, a pressurized tower reflux pump and a rectifying methanol cooler are sequentially arranged on the second pressurized rectifying tower pipeline between the pressurized tower cooler and the rectifying methanol tank area, and the pressurized tower reflux tank is connected with a pre-rectifying tower reboiler.
Preferably, the second pressurized distillation tower pipeline is connected with the third negative pressure distillation tower pipeline.
Compared with the prior art, the utility model has the advantages of as follows and positive effect:
(1) the device adopts a heat pump rectification technology, and can greatly reduce the reflux ratio of the tower and save energy consumption by arranging the negative pressure tower;
(2) a part of methanol is reserved in the tower kettle of the negative pressure rectifying tower of the device, so that the bubble point of the tower kettle material is low enough, the tower top pressurization amplitude is controlled within 150KPa, and further, a lower temperature difference is obtained, the type selection of the first compressor is easier, the actual power consumption of the first compressor is lower, and the COP value of the heat pump system is about 9.65;
(3) the device is provided with a pressurizing tower, the operating pressure of the tower is 180-300Kpa, the temperature at the top of the tower is 80-97 ℃, the requirement of a heating heat source of a pre-rectifying tower kettle reboiler can be met, the purpose of double-effect rectification is realized, and the consumption of primary steam is reduced by more than 40%;
(4) the fusel treatment device adopts a heat pump rectification technology, steam at the top of the tower is pressurized and heated by a compressor II, and then supplies heat to a reboiler I of a fusel recovery tower at the tower bottom, so that the heat load at the top of the tower is recycled, and the COP value of a heat pump system of the fusel treatment device is about 4.91;
(5) the comprehensive steam unit consumption of each ton of refined methanol of the device is 0.25-0.36 ton, and the average steam consumption of each ton of refined methanol is 0.81-1.15 ton at present, which is close to the lowest steam consumption level of the industry.
(6) The heat at the top of the negative pressure rectifying tower is recovered into low-pressure steam through the heat pump, so that the energy waste is reduced, the requirements of the national double-carbon policy are responded, and the energy conservation is realized to the greatest extent.
Drawings
FIG. 1 is a schematic structural diagram of the present application;
FIG. 2 is a schematic view of the structure of the connection of a pre-rectification column, a negative pressure rectification column and a pressurized rectification column;
FIG. 3 is a schematic view showing the construction of a wastewater treatment apparatus and a fusel treatment apparatus according to the present invention;
1. a pre-rectifying tower 2, a pipeline I3, a negative pressure rectifying tower 4 and a pipeline II
5. A pressure rectifying tower 6, a refined methanol tank area 7, a waste water evaporator 8 and a waste water pipeline
9. Waste water pump 10, waste water cooler 11, water outlet pipeline 12 and condensation cooler
13. A water outlet pipeline I14, a heater 15, a heat exchange pipeline I16 and a heat exchange pipeline II
17. Reflux pump 18, fusel recovery tower 19, fusel recovery pipeline 20 and fusel cooler
21. Fusel buffer tank 22, fusel extraction pump 23, extraction pipeline 24 and fusel recovery tower kettle pump
25. Fusel recovery tower reboiler I26, fusel recovery tower reboiler II 27 and fusel vertical buffer tank
28. Heat exchange pipeline three 29, compressor two 30 and heat exchange pipeline four
31. Crude methanol circulating pump 32, fusel cooler I33, fusel recovery tower pipeline I
34. A fusel water return tower reflux groove 35, a refined methanol cooler I36 and a fusel recovery tower pipeline II
37. Refined methanol cooler II 38, fusel reflux pump 39 and fusel recovery tower pipeline III
40. A first condenser 41 of the pre-rectifying tower, a first pipeline 42 of the pre-rectifying tower and a second condenser of the pre-rectifying tower
43. A second pre-rectifying tower pipeline 44, a second pre-gas-liquid separator 45 and a third pre-rectifying tower pipeline
46. A pre-reflux tank 47, a pre-rectifying tower reflux pipeline 48 and a pre-rectifying tower reflux pump
49. A pre-rectifying tower pipeline four 50, a negative pressure rectifying tower reboiler one 51 and a negative pressure rectifying tower reboiler two
52. Five heat exchange pipelines 53, six heat exchange pipelines 54 and negative pressure backflow tank
55. A first negative pressure distillation tower pipeline 56, a second negative pressure distillation tower pipeline 57 and a third negative pressure distillation tower pipeline
58. Negative pressure tower first cooler 59, negative pressure tower second cooler 60, interlocking control device
61. Negative pressure reflux pump 62, pressurizing tower cooler 63 and pressurizing rectification tower pipeline I
64. A second pressurized rectifying tower pipeline 65, a pressurized tower reflux tank 66 and a pressurized tower reflux pump
67. Refined methanol cooler 68, pre-rectifying tower reboiler I69, pre-rectifying tower reboiler II
70. Pre-tower vertical buffer tank 71, heat exchange pipeline seven 72 and heat exchange pipeline eight
73. A pre-tower heat exchange circulating pump 74, a pressurized rectifying tower reboiler 75 and a compressor I
76. A tower kettle circulating pump 77, a pre-rectifying tower cooler 78 and a condensed water reflux pipeline
79. Waste water pipeline I80, public end bus 81, pipeline 82 and liquid recovery pipeline
83. Condenser 84, reflux line 85, fusel tower top line
86. A pre-rectifying tower preheater.
Detailed Description
The following describes in detail an embodiment of the present invention with reference to fig. 1 to 3. It should be noted that the specific embodiments described herein are only used for illustrating and explaining the present invention, and are not used for limiting the present invention.
The first embodiment is as follows:
the embodiment provides a four-tower heat pump thermal coupling methanol rectification device, which comprises a pre-rectification tower 1, a negative pressure rectification tower 3, a pressurized rectification tower 5 and a fusel recovery tower 18 which are sequentially connected, more specifically, the bottom of the pre-rectification tower 1 is connected with a feed inlet of the negative pressure rectification tower 3 through a pipeline I2, a tower kettle circulating pump 76 and a pre-rectification tower cooler 77 are sequentially arranged on the pipeline I2 between the pre-rectification tower 1 and the negative pressure rectification tower 3, the bottom of the negative pressure rectification tower 3 is connected with the feed inlet of the pressurized rectification tower 5 through a pipeline II 4, the bottom of the negative pressure rectification tower 5 is connected with a negative pressure rectification tower reboiler I50 and a negative pressure rectification tower reboiler II 51, the top of the negative pressure rectification tower 5 is connected with the negative pressure rectification tower II 51 through a heat exchange pipeline V52, a compressor I75 is arranged on the heat exchange pipeline V52, and preferably, in order to improve stability, The reliability, compressor 75 is two at least parallelly connected compressor unit, and every compressor unit includes an at least compressor, and when one of them compressor unit goes wrong, can not lead to the unable normal work of equipment, has improved the security.
In this embodiment, the negative pressure rectification tower 3 adopts a heat pump rectification technology (which may also be referred to as a heat pump compressor rectification technology, and for convenience of description, hereinafter referred to as a heat pump rectification technology), vapor at the top of the tower is pressurized and heated by a compressor one 75, and then heat is supplied to a negative pressure rectification tower reboiler two 51, so that the heat load at the top of the tower is reused, and the COP value of the heat pump system of the negative pressure rectification tower 3 is 8-12, and more preferably 9.65; the first negative pressure rectifying tower reboiler 50 can be heated by conventional external steam, sufficient heat energy supply can be provided when the equipment is started or is operated under special conditions such as instability, the second negative pressure rectifying tower reboiler 51 is heated by steam extracted from the top of the negative pressure rectifying tower 3, and the steam enters the negative pressure reflux tank 54 after heat exchange.
The top of the pre-rectifying tower 1 is connected with a pre-rectifying tower gas treatment device, the lower part of the pre-rectifying tower 1 is provided with a pre-rectifying tower reboiler, the second negative pressure rectifying tower reboiler 51 is connected with a negative pressure rectifying tower liquid treatment device through a heat exchange pipeline six 53, the top of the pressurized rectifying tower 5 is provided with a pressurized rectifying tower gas treatment device, the pressurized rectifying tower gas treatment device is connected with a rectifying methanol tank area 6, and the rectifying methanol tank area 6 is also connected with the negative pressure rectifying tower liquid treatment device; the lower part of the pressurized rectifying tower 5 is also provided with a pressurized rectifying tower reboiler 74, and the pressurized rectifying tower reboiler 74 is heated by adopting conventional external steam to provide heat energy supply.
More specifically: the pre-rectifying tower gas treatment device comprises a pre-rectifying tower first condenser 40, wherein the pre-rectifying tower first condenser 40 is connected with a pre-rectifying tower second condenser 42 through a pre-rectifying tower pipeline I41, the pre-rectifying tower second condenser 42 is connected with a pre-gas-liquid separator 44 through a pre-rectifying tower pipeline II 43, the pre-gas-liquid separator 44 is connected with a pre-reflux groove 46 through a pre-rectifying tower pipeline III 45, the pre-reflux groove 46 is connected with the top of the pre-rectifying tower 1 through a pre-rectifying tower reflux pipeline 47, and a pre-rectifying tower reflux pump 48 is arranged on the pre-rectifying tower reflux pipeline 47; the top of the pre-reflux groove 46 is connected with a pre-rectifying tower first condenser 40 through a pre-rectifying tower pipeline four 49; the crude methanol is fully contacted with gas and liquid of a high-efficiency DVST tower plate or a plurality of sections of fillers in a pre-rectifying tower 1, light components and a small part of methanol in the crude methanol are extracted from the top of the pre-rectifying tower in a gaseous form, the light components and the small part of methanol are sequentially connected with a gas phase inlet of a first condenser 40 of the pre-rectifying tower, a gas phase inlet of a second condenser 42 of the pre-rectifying tower and a pre-gas-liquid separator 44, non-condensable gas outlets (CO, CO2, H2, N2, CH4, multi-carbon alkane, ethyl acetate, dimethyl ether and the like, 40 ℃, 0.12MPa (A), 3.0-50.0m3/H) of the second condenser 42 of the pre-rectifying tower and the pre-gas-liquid separator 44 enter a subsequent post-treatment and flare system, condensate outlets of the first condenser 40 of the pre-rectifying tower and the pre-gas-liquid separator 44 are connected into a pre-reflux tank 46, pressurized by a pre-rectifying tower reflux pump 48, enter the top of the pre-rectifying tower 1 for reflux, the pre-rectifying tower 1 and the flare system, The pre-rectifying tower second condenser 42 and the pre-gas-liquid separator 44 are provided with an interlocking control device 60 so as to control the carrying-out amount of the methanol; preferably, a first pre-rectification column line 41 between the first pre-rectification column condenser 40 and the second pre-rectification column condenser 42 is further connected with the pre-reflux tank 46 to release the excess non-condensable gas from the pre-reflux tank 46.
The negative pressure rectifying tower liquid treatment device comprises a negative pressure reflux tank 54 connected with a heat exchange pipeline six 53, the negative pressure reflux tank 54 is connected with the upper part of the negative pressure rectifying tower 3 through a negative pressure distilling tower pipeline one 55 and a negative pressure distilling tower pipeline two 56, the negative pressure reflux tank 54 is connected with the refined methanol tank area 6 through a negative pressure distilling tower pipeline one 55 and a negative pressure distilling tower pipeline three 57, and a negative pressure tower first cooler 58 and a negative pressure tower second cooler 59 are sequentially arranged on the negative pressure distilling tower pipeline three 57 between the negative pressure reflux tank 54 and the refined methanol tank area 6; the second negative pressure distillation tower pipeline 56 and the third negative pressure distillation tower pipeline 57 are both provided with a negative pressure reflux pump 61; the negative pressure backflow tank 54 is connected with a public end bus 80 connected with the first compressor 75 in parallel through a pipeline 81, a liquid recovery pipeline 82 is connected to the negative pressure backflow tank 54, the liquid recovery pipeline 82 is connected with a vacuum system, and a condenser 83 is arranged on the liquid recovery pipeline 82; preferably, an interlocking control device 60 is arranged between the liquid recovery pipeline 82 and the heat exchange pipeline five 52 and is used for controlling the top reflux quantity of the negative pressure rectifying tower 3; after light components are removed from the pre-rectifying tower 1, aqueous methanol solution is extracted from the tower bottom and enters a negative pressure rectifying tower 3, gas-liquid heat transfer and mass transfer are carried out on the gas-liquid through a high-efficiency tower tray or a filler in the negative pressure rectifying tower 3, water, ethanol, fusel alcohol and the like in the methanol are fully removed, gas phase at the tower top enters a second negative pressure rectifying tower reboiler 51 through a fifth heat exchange pipeline 52 and supplies heat to the second negative pressure rectifying tower reboiler 51, liquid phase after heat exchange flows into a negative pressure reflux tank 54, non-condensable gas enters a first negative pressure tower cooler 58 and a second negative pressure tower cooler 59 of the negative pressure tower and further condenses and then enters a rectifying methanol tank area 6 for storage; after the liquid in the negative pressure reflux tank 54 is pressurized by the negative pressure reflux pump 61, one stream of the liquid returns to the top of the negative pressure rectifying tower 3 to be used as reflux liquid, and the other stream of the liquid is cooled and then is conveyed to the refined methanol tank area 6.
The pressurized rectifying tower gas treatment device comprises a pressurized tower cooler 62, wherein the pressurized tower cooler 62 is connected with the top of a pressurized rectifying tower 5 through a pressurized rectifying tower pipeline I63, the pressurized tower cooler 62 is connected with a rectifying methanol tank area 6 through a pressurized rectifying tower pipeline II 64, and a pressurized tower reflux tank 65, a pressurized tower reflux pump 66 and a rectifying methanol cooler 67 are sequentially arranged on the pressurized rectifying tower pipeline II 64 between the pressurized tower cooler 62 and the rectifying methanol tank area 6; preferably, a second pressurized rectifying tower pipeline 64 at the rear section of the refined methanol cooler 67 is connected with a third negative pressure distillation tower pipeline 57, and the refined methanol formed after condensation at the top of the pressurized rectifying tower 5 and the refined methanol condensed at the upper part of the negative pressure rectifying tower 3 are jointly conveyed to the refined methanol tank area 6; and a second pressurized rectifying tower pipeline 64 between the pressurized tower reflux pump 66 and the refined methanol cooler 67 is connected with the top of the negative pressure rectifying tower 5 through a reflux pipeline 84.
The pre-rectifying tower reboiler comprises a pre-rectifying tower reboiler I68 and a pre-rectifying tower reboiler II 69, a pre-rectifying tower vertical buffer tank 70 is arranged at the front part of the pre-rectifying tower reboiler I68, the pre-rectifying tower vertical buffer tank 70 is connected with a pressurized rectifying tower pipeline I63 through a heat exchange pipeline seven 71, and the tower vertical buffer tank 70 is further connected with a pressurized rectifying tower reflux tank 65 through a heat exchange pipeline eight 72; a pre-tower heat exchange circulating pump 73 is arranged on the heat exchange pipeline eight 72; a part of steam at the top of the pressurized rectifying tower 3 enters a pre-tower vertical buffer tank 70, flows out through a pre-tower heat exchange circulating pump 73 and enters a pressurized tower reflux tank 65 through a heat exchange pipeline eight 75; the safety of steam heat exchange and the stability of heat exchange heat after pressurization are improved by indirect heat exchange between the pre-tower vertical buffer tank 70 and the pre-rectifying tower reboiler I68; an interlocking control device 60 is arranged between the pre-tower vertical buffer tank 70 and the heat exchange pipeline eight 72, so that the material flow of heat exchange circulation is controlled; the second pre-rectifying tower reboiler 69 can be heated by conventional external steam, and can provide sufficient heat energy when the equipment is started or is operated unstably and other special conditions.
The bottom of pressurization rectifying column 5 still is connected with pressurization rectifying column reboiler 74, pre-rectifying column reboiler two 69, pressurization rectifying column reboiler 74, negative pressure rectifying column reboiler 50, fusel recovery column reboiler two 26 supply heat through external firing equipment, can supply heat through an external firing equipment, also can supply heat respectively, the technical staff carry on corresponding selection according to particular case can, this application does not do specifically prescribe a limit to.
In the embodiment, the total process route is the sequence of the pre-rectifying tower 1, the negative pressure rectifying tower 3, the pressurizing rectifying tower 5 and the fusel recovery tower 18, the methanol is purified, the waste heat evaporation and the recycling of condensed water of wastewater are combined, thermal coupling is fully performed, the energy-saving advantage of a heat pump technology is exerted, the pressure and the difficulty of a wastewater treatment section are reduced while the methanol is purified, the average steam consumption of each ton of refined methanol is lower than the lowest steam consumption level of the industry, the energy consumption is saved, the energy waste is reduced, the requirements of the national dual-carbon energy-saving policy are responded, and the energy conservation is realized to the greatest extent; the comprehensive steam unit consumption of each ton of refined methanol of the device is 0.25-0.36 ton, the average steam consumption of each ton of refined methanol is 0.81-1.15 ton at present, and the average steam consumption of each ton of refined methanol is lower than the lowest steam consumption level of the industry through the arrangement of the device.
Example two:
in this embodiment, the measurement line of the pressurized rectifying tower 5 is connected to a fusel recovery tower 18, which is used for processing fusel extracted from the pressurized rectifying tower 5, specifically:
a fusel recovery tower 18 is connected with a pressurized rectifying tower 5 through a fusel recovery pipeline 19, a fusel cooler 20, a fusel buffer tank 21 and a fusel extraction pump 22 are sequentially arranged on the fusel recovery pipeline 19 between the pressurized rectifying tower 5 and the fusel recovery tower 18, the top of the fusel recovery tower 18 is connected with a methanol gas treatment device, the lower part of the fusel recovery tower 18 is connected with a wastewater treatment device through an extraction pipeline 23, and a fusel recovery tower kettle pump 24 is arranged on the extraction pipeline 23; the bottom of the fusel recovery tower 18 is also connected with a first fusel recovery tower reboiler 25 and a second fusel recovery tower reboiler 26, the first fusel recovery tower reboiler 25 is connected with a vertical fusel buffer tank 27, the vertical fusel buffer tank 27 is connected with the top of the fusel recovery tower 18 through a third heat exchange pipeline 28 and a top pipeline 85 of the fusel tower, the third heat exchange pipeline 28 is provided with a second compressor 29, the vertical fusel buffer tank 27 is also connected with a methanol gas treatment device through a fourth heat exchange pipeline 30, and the fourth heat exchange pipeline 30 is provided with a crude methanol circulating pump 31; preferably, the second compressor 29 is at least two parallel compressor sets, and each compressor set comprises at least one compressor.
The fusel extracted from a side port of a pressurized rectifying tower 5 enters a fusel recovery tower 18 through a fusel cooler 20, a fusel buffer tank 21 and a fusel extraction pump 22 to be rectified and purified, part of gas extracted from the top is used for supplying heat to a reboiler I25 of the fusel recovery tower, and the other part of gas is treated by a methanol gas treatment device, the fusel liquid extracted from the side line contains 30-40% of methanol, and after the fusel liquid is injected into the fusel recovery tower 18, organic matters such as methanol, ethanol, isopropanol, butanol and the like in the fusel liquid are recovered and can be used as fuel, so that fuel methanol is obtained; the second fusel recovery tower reboiler 26 is heated by external conventional steam equipment and the like, and can provide sufficient heat energy supply when the equipment is started or is operated under special conditions such as unstable operation and the like.
In the embodiment, the fusel recovery tower 18 adopts a heat pump rectification technology, steam at the top of the tower is pressurized and heated by a compressor II 29, and then heat is supplied to a reboiler I25 of the fusel recovery tower, so that the heat load at the top of the tower is recycled, and the COP value of a heat pump system of the fusel recovery tower 18 is about 4.91; indirect heat exchange is carried out through the fusel vertical buffer tank 27 and the fusel recovery tower reboiler I25, and the safety of steam heat exchange and the stability of heat exchange heat after pressurization are improved.
Example three:
the present embodiment describes a methanol gas processing apparatus, specifically:
the methanol gas treatment device comprises a fusel cooler I32 connected with a top pipeline 85 of a fusel tower, the fusel cooler I32 is connected with a fusel water returning tower reflux tank 34 through a fusel recovery tower I33, the fusel recovery tower I33 is connected with a heat exchange pipeline IV 30, the fusel water returning tower reflux tank 34 is connected with a refined methanol cooler I35, the fusel water returning tower reflux tank 34 is also connected with a refined methanol cooler II 37 through a fusel recovery tower II 36, a fusel reflux pump 38 is arranged on the fusel recovery tower II 36, and the recovery tower II 36 is connected with the upper part of the fusel recovery tower 18 through a recovery tower III 39.
The gas phase at the top of the fusel recovery tower 18 passes through a fusel cooler I32, a return water tower reflux tank 34 and a refined methanol cooler 37, and organic matters such as methanol, ethanol, isopropanol, butanol and the like in the gas phase are recovered and can be used as fuel, namely the fuel methanol.
Example four:
this example describes a wastewater treatment plant, specifically:
the bottom of the pressurized rectifying tower 5 is connected with a wastewater treatment device, the wastewater treatment device comprises a wastewater evaporator 7, the wastewater evaporator 7 is connected with the extraction pipeline 23, the wastewater evaporator 7 is connected with the bottom of the pressurized rectifying tower 5 through a wastewater pipeline 8, a wastewater pump 9 is arranged on the wastewater pipeline 8, the top of the wastewater evaporator 7 is connected with a water outlet pipeline 11, and a condensation cooler 12 is arranged on the water outlet pipeline 11; a water outlet pipeline I13 is arranged at the bottom of the waste water evaporator 7; the liquid at the bottom of the pressurized rectifying tower 5 enters a wastewater evaporator 7, after heating and evaporation, the gas phase is cooled by a condensing cooler 12 to form pure water for collection, and the unevaporated part conveys the wastewater to a sewage treatment plant for biochemical treatment through a water outlet pipeline I13; the waste water evaporator 7 is also connected with a heater 14, the heater 14 is used for supplying heat to the waste water evaporator 7, the heater 14 is connected with the top of the pre-rectifying tower 1 through a heat exchange pipeline I15, and gas phase at the top of the pre-rectifying tower 1 supplies heat to the heater 14 so as to heat the waste water evaporator 7; the heater 14 is connected with the pre-rectifying tower gas treatment device through a second heat exchange pipeline 16, more specifically, the heater 14 is connected with a fourth pre-rectifying tower pipeline 49 through the second heat exchange pipeline 16, and a reflux pump 17 is arranged on the second heat exchange pipeline 16; more specifically: the condensate obtained by evaporating the wastewater is fed into the pre-reflux tank 46 of the pre-rectifying tower through the second 16 and fourth 49 pipelines to be used as extraction water.
Most of the components discharged from the waste water evaporator 7 are water, but contain a small amount of methanol and fusel alcohol such as isopropanol and butanol, and the condensed components are returned to the reflux tank 46 of the pre-rectifying tower, so that on one hand, the recovered methanol and fusel alcohol reduce the loss of useful materials, on the other hand, the difficulty and cost of sewage treatment are reduced, and the beneficial effects of reducing the consumption of soft water and realizing the saving of water resources are achieved.
Preferably, the first wastewater line 79 is further connected to the first wastewater line 8, a wastewater cooler 10 is arranged on the first wastewater line 79, and wastewater flows out of the biochemical system through the first wastewater line 79 to be treated after being cooled by the wastewater cooler 10.
Preferably, the water outlet line 11 is further connected to a condensed water return line 78, the condensed water return line 78 is connected to a pre-rectifying column gas treatment plant connected to the pre-rectifying column top 1, more specifically, the condensed water return line 78 is connected to the pre-reflux tank 46, and a part of the evaporated condensed water is returned to the pre-reflux tank 46 to be used as extract water.
In this embodiment, the liquid generated at the bottom of the pressurized rectifying tower 5 is treated to obtain pure water; and the heat at the top of the negative pressure pre-rectifying tower 3 is recovered into low-pressure steam through the second negative pressure rectifying tower reboiler 51, so that the energy waste is reduced, the double-carbon requirement is met, and the energy conservation is realized to the greatest extent.
The utility model discloses a concrete theory of operation does: crude methanol enters the pre-rectifying tower 1 through a pre-rectifying tower preheater 86 and is fully contacted with gas liquid through a high-efficiency DVST tower plate or a plurality of sections of fillers in the pre-rectifying tower, light components in the crude methanol and a small part of methanol are extracted from the top of the pre-rectifying tower 1 in a gaseous state, a part of the gaseous state is sequentially connected with a pre-rectifying tower first condenser 40, a gas phase inlet of a pre-rectifying tower second condenser 42 and a pre-gas-liquid separator 44, non-condensable gas outlets (CO, CO2, H2, N2, CH4, multi-carbon alkane, ethyl acetate, dimethyl ether and the like, 40 ℃, 0.12MPa (A) and 3.0-50.0m3/H) of the pre-rectifying tower second condenser 42 and the pre-gas-liquid separator 44 enter a subsequent post-treatment and torch system, condensate outlets of the pre-rectifying tower first condenser 40 and the pre-gas-liquid separator 44 are connected and enter a pre-reflux groove 46, are pressurized through a pre-rectifying tower reflux pump 48 and then enter the top of the pre-rectifying tower plate 1 for reflux, a linkage control device 60 is arranged between the top of the pre-rectifying tower 1 and the flare system; a part of gas state provides a heat source for the heater 14 through a first heat exchange pipeline 15; crude methanol is subjected to light component impurities such as acetone and dimethyl ether removal through a pre-rectifying tower 1, then enters a negative pressure rectifying tower 3 through a pipeline I2, steam on the top of the negative pressure rectifying tower 3 is pressurized through a compressor I75, is sprayed into a saturated state through methanol per se, then enters a negative pressure rectifying tower reboiler II 51 to provide a heat source for the negative pressure rectifying tower reboiler II 51, a liquid phase after heat exchange flows into a negative pressure reflux tank 54, a part of non-condensable gas enters a negative pressure tower first cooler 58 and a negative pressure tower first cooler 59 for further condensation, then enters a refined methanol tank area 6 for storage, and the other part of non-condensable gas enters a vacuum system after being cooled through a condenser 83; after being pressurized by the negative pressure reflux pump 61, the liquid in the negative pressure reflux tank 54 returns to the top of the negative pressure rectifying tower 3 to be used as reflux; the liquid at the bottom of the pressurized rectifying tower 5 enters a wastewater evaporator 7, after heating and evaporation, the gas phase is cooled by a condensing cooler 12 to form pure water for collection, and the unevaporated part conveys the wastewater to a sewage treatment plant for biochemical treatment through a water outlet pipeline I13; the liquid at the bottom of the pressurized rectifying tower 5 can also be directly cooled by a wastewater cooler 10 on a wastewater pipeline I79 and then enters a biochemical system for treatment; the heater 14 connected with the waste water evaporator 7 is used for supplying heat to the waste water evaporator 7, the gas generated at the top of the pre-rectifying tower 1 provides a heat source for the heater 14, so that the waste water evaporator 7 is heated, the fusel extracted from the side line port of the pressurized rectifying tower 5 enters the fusel recovery tower 18 through the fusel cooler 20, the fusel buffer tank 21 and the fusel extraction pump 22 for rectification and purification, one part of the gas extracted from the top is used for supplying heat to the second reboiler 26 of the fusel recovery tower, and the other part of the gas is treated by the methanol gas treatment device, the fusel liquid extracted from the side line contains 30-40% of methanol, and after the gas is injected into the fusel recovery tower 18, the organic matters such as methanol, ethanol, isopropanol, butanol and the like are recovered and can be used as fuel.
The application can directly improve the traditional three-tower downstream double-effect process in the prior art:
such as: in a certain methanol plant, a traditional three-tower cocurrent double-effect process is adopted, the feeding amount is 71.1t/h, and when the operation parameters reach the best, the energy consumption is 1.25 tons of steam/refined methanol.
In order to reduce the consumption of methanol steam, a negative pressure rectifying tower 3 is additionally arranged by adopting a four-tower heat pump thermal coupling rectifying line, the methanol steam at the tower top of a pressurized rectifying tower 5 provides a heat source for a pre-rectifying tower reboiler 68, the methanol steam at the tower top of a negative pressure rectifying tower 50 of the negative pressure rectifying tower 3 adopts the methanol steam at the tower top of the negative pressure rectifying tower 50, the negative pressure rectifying tower reboiler is pressurized and heated by a compressor 75, the negative pressure rectifying tower is recycled, the steam energy consumption is saved by 68t/h, the 75 electric energy consumption of the compressor is considered to be 4550kw, and the COP value of the heat pump reaches about 8.6; the normal steam consumption of the pre-rectifying tower 1 is 17.14 tons/h, during the start-up debugging process, the gas-phase refined methanol steam at the top of the pressurized rectifying tower 5 supplies heat for a newly added pre-rectifying tower reboiler I68, the addition of the water steam in the pre-rectifying tower 1 is gradually reduced, finally, the water steam consumption of the pre-rectifying tower 1 is reduced to zero, and high-quality refined methanol can be produced at the top of the tower, wherein the proportion of the refined methanol in the total refined methanol is about 17.44%;
the fusel recovery tower 18 adopts a heat pump rectification mode, the compression power consumption is 350Kw, no steam is consumed, the comprehensive water vapor consumption of the refined methanol is 0.31-0.35 t/ton of the refined methanol, the power consumption is 0.6 yuan/kw.h according to the electricity fee, the steam price is 200 yuan/ton, the steam consumption per ton of the refined methanol is 0.24 ton of steam, and the comprehensive consumption is 0.55-0.59 ton of steam/ton of the refined methanol. With the increase of carbon trading price, the steam price can further rise, the technical development of new energy resources and the electricity price can further fall, and the comprehensive benefit of the process can be more obvious.
In conclusion, owing to adopted above-mentioned technical scheme, the utility model has the advantages of as follows and positive effect:
the device adopts a heat pump rectification technology, and can greatly reduce the reflux ratio of the tower and save energy consumption by arranging the negative pressure tower;
(2) a part of methanol is reserved in the tower kettle of the negative pressure rectifying tower of the device, so that the bubble point of the tower kettle material is low enough, the tower top pressurization amplitude is controlled within 150KPa, and further, a lower temperature difference is obtained, the type selection of the first compressor is easier, the actual power consumption of the first compressor is lower, and the COP value of the heat pump system is about 9.65;
(3) the device is provided with a pressurizing tower, the operating pressure of the pressurizing tower is 180-300Kpa, the temperature at the top of the tower is 80-97 ℃, the requirement of a heating heat source of a reboiler at the bottom of the pre-rectifying tower can be met, the purpose of double-effect rectification is realized, and the consumption of primary steam is reduced by more than 40%;
(4) the fusel treatment device adopts a heat pump rectification technology, steam at the tower top is pressurized and heated by a compressor II, and then heat is supplied to a reboiler I of a fusel recovery tower at a tower kettle, so that the heat load at the tower top is recycled, and the COP value of a heat pump system of the fusel treatment device is about 4.91;
(5) the comprehensive steam unit consumption of each ton of refined methanol of the device is 0.25-0.36 ton, and the average steam consumption of each ton of refined methanol is 0.81-1.15 ton at present, which is close to the lowest steam consumption level in the industry.
(6) The heat at the top of the negative pressure rectifying tower is recovered into low-pressure steam through the heat pump, so that the energy waste is reduced, the requirements of the national double-carbon policy are responded, and the energy conservation is realized to the greatest extent.
The device, the connection relation etc. that above-mentioned not specifically describe all belong to prior art, the utility model discloses do not do specific repeated description here.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited to the details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are included in the scope of protection of the present invention.
It should be noted that, in the foregoing embodiments, various features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various combinations that are possible in the present application will not be described separately.
In addition, any combination of the various embodiments of the present application can be made, and the present application should be considered as disclosed in the present application as long as the combination does not depart from the spirit of the present application.
Claims (10)
1. The four-tower heat pump thermal coupling methanol rectification device is characterized by comprising a pre-rectification tower (1), a negative pressure rectification tower (3), a pressurizing rectification tower (5) and a fusel recovery tower (18) which are sequentially connected, wherein a negative pressure rectification tower reboiler I (50) and a negative pressure rectification tower reboiler II (51) are connected to the bottom of the negative pressure rectification tower (3), the top of the negative pressure rectification tower (3) is connected with the negative pressure rectification tower reboiler II (51) through a heat exchange pipeline V (52), and a compressor I (75) is arranged on the heat exchange pipeline V (52).
2. The four-tower heat pump thermally coupled methanol rectification device according to claim 1, characterized in that a first fusel recovery tower reboiler (25) and a second fusel recovery tower reboiler (26) are connected to the bottom of the fusel recovery tower (18), the first fusel recovery tower reboiler (25) is connected to a first fusel vertical buffer tank (27), the first fusel vertical buffer tank (27) is connected to the top of the fusel recovery tower (18) through a third heat exchange line (28) and a top fusel tower pipeline (85), a second compressor (29) is arranged on the third heat exchange line (28), the vertical fusel buffer tank (27) is further connected to a methanol gas treatment device through a fourth heat exchange line (30), and a crude methanol circulating pump (31) is arranged on the fourth heat exchange line (30).
3. The thermally coupled methanol rectification device with the four-tower heat pump as recited in claim 1 is characterized in that a pre-rectification tower gas treatment device is connected to the top of the pre-rectification tower (1), a pre-rectification tower reboiler I (68) and a pre-rectification tower reboiler II (69) are arranged at the lower part of the pre-rectification tower (1), and the pre-rectification tower reboiler I (68) is connected with a pressurized rectification tower pipeline I (63) at the top of a pressurized rectification tower (5) through a heat exchange pipeline seven (71); the second negative pressure rectifying tower reboiler (51) is connected with a negative pressure rectifying tower liquid treatment device through a heat exchange pipeline six (53), the top of the pressurized rectifying tower (5) is provided with a pressurized rectifying tower gas treatment device, the pressurized rectifying tower gas treatment device is connected with a rectifying methanol tank area (6), and the rectifying methanol tank area (6) is also connected with the negative pressure rectifying tower liquid treatment device; and a pressurized rectifying tower reboiler (74) is also arranged at the lower part of the pressurized rectifying tower (5).
4. The thermally coupled methanol rectification device with the four-tower heat pump as recited in claim 2 is characterized in that the first compressor (75) and the second compressor (29) are respectively at least two compressor sets connected in parallel, and each compressor set at least comprises one compressor.
5. The four-tower heat pump thermally coupled methanol rectification device of claim 2, wherein, the methanol gas treatment device comprises a fusel cooler I (32) connected with a heat exchange pipeline III (28) and a fusel tower top pipeline (85), the fusel cooler I (32) is connected with a fusel water return tower reflux tank (34) through a fusel recovery tower pipeline I (33), the fusel recovery tower pipeline I (33) is connected with the heat exchange pipeline IV (30), the fusel water return tower reflux tank (34) is connected with a refined methanol cooler I (35), the fusel water returning tower reflux tank (34) is also connected with a refined methanol cooler II (37) through a fusel recovery tower pipeline II (36), a fusel reflux pump (38) is arranged on the fusel recovery tower pipeline II (36), the fusel recovery tower pipeline II (36) is connected with the upper part of the fusel recovery tower (18) through a fusel recovery tower pipeline III (39).
6. The thermally coupled methanol rectification plant with a four-tower heat pump according to claim 1 is characterized in that the bottom of the pressurized rectification tower (5) and the bottom of the fusel recovery tower (18) are connected with a wastewater treatment device.
7. The four-tower heat pump thermally coupled methanol rectification device of claim 6, wherein, the wastewater treatment device comprises a wastewater evaporator (7), the wastewater evaporator (7) is connected with the bottom of the pressurized rectifying tower (5) through a wastewater pipeline (8), a waste water pump (9) is arranged on the waste water pipeline (8), the top of the waste water evaporator (7) is connected with a water outlet pipeline (11), a condensation cooler (12) is arranged on the water outlet pipeline (11), a water outlet pipeline I (13) is arranged at the bottom of the waste water evaporator (7), the waste water evaporator (7) is also connected with a heater (14), the heater (14) is connected with the top of the pre-rectifying tower (1) through a heat exchange pipeline I (15), the heater (14) is connected with the pre-rectifying tower gas treatment device through a second heat exchange pipeline (16); the waste water evaporator (7) is connected with the bottom of the fusel recovery tower (18) through a production pipeline (23).
8. A four-column heat pump thermally coupled methanol rectification plant according to claim 7 characterized in that the water outlet line (11) is further connected to a condensed water return line (78), the condensed water return line (78) being connected to the pre-rectification column gas treatment plant.
9. The four-tower heat pump thermal coupling methanol rectification device according to claim 8, characterized in that the pre-rectification tower gas treatment device comprises a pre-rectification tower first condenser (40), the pre-rectification tower first condenser (40) is connected with a pre-rectification tower second condenser (42) through a pre-rectification tower pipeline I (41), the pre-rectification tower second condenser (42) is connected with a pre-gas-liquid separator (44) through a pre-rectification tower pipeline II (43), the pre-gas-liquid separator (44) is connected with a pre-reflux tank (46) through a pre-rectification tower pipeline III (45), the pre-reflux tank (46) is connected with the top of the pre-rectification tower (1) through a pre-rectification tower reflux pipeline (47), and a pre-rectification tower reflux pump (48) is arranged on the pre-rectification tower reflux pipeline (47); the top of the pre-reflux groove (46) is connected with a first condenser (40) of the pre-rectifying tower through a pre-rectifying tower pipeline four (49); the pre-return tank (46) is connected to the water outlet line (11) via the condensate return line (78).
10. The four-tower heat pump thermally coupled methanol rectification device according to claim 3, characterized in that the negative pressure rectification tower liquid treatment device comprises a negative pressure reflux tank (54) connected with a heat exchange pipeline six (53), the negative pressure reflux tank (54) is connected with the upper part of the negative pressure rectification tower (3) through a negative pressure distillation tower pipeline one (55) and a negative pressure distillation tower pipeline two (56), the negative pressure reflux tank (54) is connected with the refined methanol tank area (6) through a negative pressure distillation tower pipeline one (55) and a negative pressure distillation tower pipeline three (57), and a negative pressure tower first cooler (58) and a negative pressure tower second cooler (59) are sequentially arranged on the negative pressure distillation tower pipeline three (57) between the negative pressure reflux tank (54) and the refined methanol tank area (6); a negative pressure reflux pump (61) is arranged on the negative pressure distillation tower pipeline II (56) and the negative pressure distillation tower pipeline III (57); the negative pressure backflow tank (54) is connected with a public end bus (80) through a pipeline (81), a liquid recovery pipeline (82) is connected to the negative pressure backflow tank (54), the liquid recovery pipeline (82) is connected with a vacuum system, and a condenser (83) is arranged on the liquid recovery pipeline (82).
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