CN216404258U - Decompression type five-tower four-effect methanol rectification device - Google Patents
Decompression type five-tower four-effect methanol rectification device Download PDFInfo
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- CN216404258U CN216404258U CN202121779130.1U CN202121779130U CN216404258U CN 216404258 U CN216404258 U CN 216404258U CN 202121779130 U CN202121779130 U CN 202121779130U CN 216404258 U CN216404258 U CN 216404258U
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Abstract
The utility model provides a decompression type five-tower four-effect methanol rectifying device, which comprises: the system comprises a pre-rectifying tower, a pressurizing tower, an atmospheric tower, a pressure reducing tower, a recovery tower, a matched reboiler, a heat exchanger, a connecting pipeline, and necessary control valves and connecting parts on the pipeline; the device adopts the mode operation of five towers four effects, effectively reduces steam consumption through multiple thermal coupling. By adopting the pressure-reducing five-tower four-effect methanol rectifying device, the steam consumption of each ton of refined methanol products is about 0.75 ton, the consumption of circulating water is 43 tons, and compared with the traditional 3+1 tower flow, the consumption of the steam is obviously reduced by 1.25 tons of refined methanol products and 75 tons of circulating water is obviously reduced by one ton of refined methanol products.
Description
Technical Field
The utility model relates to a methanol rectifying device, in particular to a pressure-reduction five-tower four-effect methanol rectifying device.
Background
Methanol is one of basic organic raw materials and is used for manufacturing various organic products such as acetic acid and the like. The main production mode at present is a synthesis method, coal is used as a raw material, the coal is gasified to obtain synthesis gas, the synthesis gas further passes through a water gas shift unit and a purification unit to obtain raw material gas required by methanol synthesis, the raw material gas passes through a synthesis reaction unit to obtain crude methanol, and the crude methanol is further rectified (rectification section) to obtain refined methanol.
The traditional methanol rectification flow of the 3+1 tower is three-tower double-effect rectification, and the three towers are a pre-rectification tower, a pressurization tower and an atmospheric tower respectively. In order to improve the yield, a recovery tower is additionally arranged, fusel (the content of methanol is 30-50%) which is detected and extracted in an atmospheric tower is rectified, the methanol in the fusel is recovered, and the yield is improved. The heat sources of the pre-rectifying tower, the pressurizing tower and the recovery tower are steam, the operating pressure of the pressurizing tower during normal production is 0.5-0.8MPa (G), the tower top temperature is about 125-. The methanol product is extracted from the tops of the pressurizing tower and the atmospheric tower in a ratio of about 1: l, about 50 percent of the methanol is generated by consuming steam in the pressurizing tower, the rest 50 percent of the methanol is generated by heating the gas phase extracted from the top of the pressurizing tower, about half of the methanol is not generated by steam, and the steam energy consumption of the method is 1.2 to 1.3 tons per ton of refined alcohol.
The document of application No. 200910022575.2 discloses a multi-effect rectification apparatus for methanol, which mainly comprises a pre-rectification column, a pressurizing column 1, a pressurizing column 2, an atmospheric column and a recovery column. Wherein, the tower top steam of the pressurized tower 1 is used as a heat source of a reboiler of the pressurized tower 2, and the tower top steam of the pressurized tower 2 is used as a heat source of a reboiler of the atmospheric tower. In addition, the steam at the top of the recovery tower is used as a heat source of a reboiler at the bottom of the pre-rectifying tower. The process is essentially a derivative of the traditional 3+1 tower process, and on one hand, the added pressurizing tower 1 needs higher pressure than the pressurizing tower in the original 3+1 tower process, so that the equipment investment of the pressurizing tower 1 is larger. On the other hand, the device cannot fully utilize the heat of the gas and the steam condensate at the top of the atmospheric tower, and the energy consumption cannot be further reduced.
The document of application No. 201010117891.0 discloses a heat pump distillation process for methanol. The process is mainly characterized in that on the basis of the traditional 3+1 tower process, the temperature and the pressure of the tower top gas of the normal pressure tower are increased, the compressed refined methanol gas is used as a heat source of a reboiler of the tower kettle of the normal pressure tower, and the comprehensive energy consumption is effectively reduced. However, the process introduces a methanol vapor compressor which is a movable device, on one hand, the investment of the previous device and the operation and maintenance cost in the operation process are increased, and on the other hand, once the compressor fails in the operation process, the rectification is stopped, and the operation stability of the device is poor.
The document of application No. 201911405716.9 discloses a five-tower four-effect methanol rectification process and equipment, which is mainly characterized by adopting three pressurized towers (a first pressurized tower, a second pressurized tower and a third pressurized tower) and a recovery tower. Wherein the heat source of the reboiler of the pre-rectifying tower is the gas phase extracted from the top of the second pressurized tower. The heat source of the reboiler of the first pressurized tower is the gas phase at the top of the third pressurized tower. The heat source of the reboiler of the second pressurized tower is the gas phase at the top of the first pressurized tower. The heat source of the reboiler of the third pressurized tower is high-pressure external steam. The design pressure of three pressurized towers in the process at least needs 800KPaG, 600KPaG and 2000KPaG, and the equipment investment is high. In addition, the process cannot fully utilize the heat of the steam condensate, and the energy consumption cannot be further reduced.
SUMMERY OF THE UTILITY MODEL
In view of the above disadvantages of the prior art, the present invention provides a pressure reduction type five-tower four-effect methanol rectification apparatus, which is used for solving the problems of poor operation stability, high cost and high energy consumption of the apparatus in the prior art.
In order to achieve the above objects and other related objects, the present invention provides a pressure-reducing five-tower four-effect methanol rectification apparatus, which mainly comprises: a crude methanol preheater, a pre-rectifying tower and a pre-rectifying tower reboiler, a pressurized tower and a pressurized tower reboiler, an atmospheric tower and an atmospheric tower reboiler, a vacuum tower and a vacuum tower reboiler, a recovery tower and a recovery tower reboiler. Wherein: the crude methanol preheater is communicated with a total feeding pipeline, a feeding hole of the pre-rectifying tower is communicated with the crude methanol preheater, a feeding hole of the pressurizing tower is communicated with a heavy component outlet of the pre-rectifying tower, a feeding hole of the normal pressure tower is communicated with a heavy component outlet of the pressurizing tower, a feeding hole of the pressure reducing tower is communicated with a heavy component outlet of the normal pressure tower, a feeding hole of the recovery tower is communicated with a heavy component outlet of the pressure reducing tower, and a heavy component outlet of the recovery tower is communicated with a wastewater discharge pipeline.
Further, the crude methanol preheater comprises a material flow pipeline and a heat source pipeline, wherein the material flow pipeline is communicated with the main feeding pipeline.
Further, in the pre-rectifying tower and the pre-rectifying tower reboiler, the pre-rectifying tower comprises a light component outlet and a heavy component outlet, the pre-rectifying tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the pre-rectifying tower, and a steam condensate outlet of the heat source pipeline is communicated with a heat source pipeline inlet of the crude methanol preheater.
Further, in the pressurizing tower and the pressurizing tower reboiler, the pressurizing tower comprises a light component outlet and a heavy component outlet, the pressurizing tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the pressurizing tower, and a steam condensate outlet of the heat source pipeline is communicated with a heat source pipeline inlet of the pre-rectifying tower reboiler.
Further, in the atmospheric tower and the atmospheric tower reboiler, the atmospheric tower comprises a light component outlet and a heavy component outlet, the atmospheric tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the atmospheric tower, an inlet of the heat source pipeline is communicated with the light component outlet of the pressurizing tower, and a steam condensate outlet of the heat source pipeline is communicated with the pressurizing tower through a pressurizing tower reflux tank.
Further, in the vacuum tower and the vacuum tower reboiler, the vacuum tower comprises a light component outlet and a heavy component outlet, the vacuum tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the vacuum tower, the vacuum tower reboiler is divided into a first vacuum tower reboiler and a second vacuum tower reboiler, the heat source pipeline of the first vacuum tower reboiler is communicated with the pre-rectifying tower, the heat source pipeline of the second vacuum tower reboiler is communicated with the atmospheric tower, and the light component outlet of the vacuum tower T04 is communicated with the vacuum tower T04 through an overhead condenser E12 and a vacuum tower reflux tank V04.
Further, in the recovery tower and the reboiler of the recovery tower, the recovery tower comprises a light component outlet and a heavy component outlet, the reboiler of the recovery tower comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the recovery tower, a steam condensate outlet of the heat source pipeline is communicated with a heat source pipeline inlet of the crude methanol preheater, the light component outlet of the recovery tower is communicated with a heat source pipeline inlet of the pre-rectifying tower reboiler, and a steam condensate outlet of the heat source pipeline of the pre-rectifying tower reboiler is communicated with the recovery tower through a recovery tower reflux tank.
As mentioned above, the decompression type five-tower four-effect methanol rectification device is reasonable in arrangement, low in consumption of pipeline materials, convenient to operate and maintain, high in operation stability, low in energy consumption and low in operation cost; compared with the traditional 3+1 tower with the same scale, the decompression type five-tower four-effect methanol rectifying device has the advantages that the decompression tower is added, and the product extraction tower is changed from the original pressurizing tower and the original normal pressure tower into the pressurizing tower, the normal pressure tower and the decompression tower, so that the product extraction proportion is more reasonable, and the influence on the whole rectifying system due to unqualified quality of methanol products in the pressurizing tower or the normal pressure tower is reduced; and because the loads of the pressurizing tower and the atmospheric tower are reduced, the equipment sizes of the pressurizing tower and the atmospheric tower can be reduced. The pressure-reducing five-tower four-effect methanol rectifying device provided by the utility model can be used for rectifying methanol by recycling heat energy, so that the heat of steam condensate is fully utilized, and the purpose of saving energy consumption is achieved.
Drawings
FIG. 1 is a schematic view of a pressure-reducing five-tower four-effect methanol rectifying apparatus according to the present invention.
FIG. 2 is a schematic diagram of the evolution device of the pressure-reducing five-tower four-effect methanol rectification device of the utility model.
In the figure, T01, pre-rectification column; t02, pressurized column; t03, atmospheric tower; t04, vacuum tower; t05, a recovery tower; e01, a crude methanol preheater; e02, a first pre-rectification column reboiler; e03, a second pre-rectifying tower reboiler; e04, third pre-rectification column reboiler; e05, a pre-tower overhead cooler; e06, pressurized column reboiler; e07, pressurized column product cooler; e08, an atmospheric tower reboiler; e09, an atmospheric tower product cooler; e10, a first decompression column reboiler; e11, a second decompression column reboiler; e12, overhead condenser; e13, a recovery tower reboiler; e14, mixed alcohol product cooler; v01, a pre-rectifying tower reflux tank; v02, pressure column reflux drum; v03, atmospheric tower reflux tank; v04, decompression tower reflux tank; v05, a recovery tower reflux tank; v06, vacuum buffer tank; p01, pre-rectifying tower reflux pump; p02, prognostic pump; p03, pressurized column reflux pump; p04, a first tower kettle pump;
p05, atmospheric tower reflux pump; p06, a second tower kettle pump; p07, vacuum tower reflux pump; p08, a third tower kettle pump; p09, a recovery tower reflux pump; p10, a fourth tower kettle pump; p11, vacuum pump.
Detailed Description
The embodiments of the present invention are described below with reference to specific embodiments, and other advantages and effects of the present invention will be easily understood by those skilled in the art from the disclosure of the present specification. The utility model is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention.
Please refer to fig. 1 and 2. It should be noted that the drawings provided in the present embodiment are only for illustrating the basic idea of the present invention, and the components related to the present invention are only shown in the drawings rather than drawn according to the number, shape and size of the components in actual implementation, and the type, quantity and proportion of the components in actual implementation may be changed freely, and the layout of the components may be more complicated.
As shown in fig. 1, an embodiment of the present invention provides a pressure-reduction five-tower four-effect methanol rectification apparatus, which mainly includes: a crude methanol preheater E01, a pre-rectifying tower T01 and a pre-rectifying tower reboiler, a pressurized tower T02 and a pressurized tower reboiler, an atmospheric tower T03 and an atmospheric tower reboiler, a vacuum tower T04 and a vacuum tower reboiler, a recovery tower T05 and a recovery tower reboiler; wherein: the crude methanol preheater E01 is communicated with a total feeding pipeline, the feed inlet of the pre-rectifying tower T01 is communicated with the crude methanol preheater E01, the feed inlet of the pressurizing tower T02 is communicated with the heavy component outlet of the pre-rectifying tower T01, the feed inlet of the atmospheric tower T03 is communicated with the heavy component outlet of the pressurizing tower T02, the feed inlet of the pressure reducing tower T04 is communicated with the heavy component outlet of the atmospheric tower T03, the feed inlet of the recovery tower T05 is communicated with the heavy component outlet of the pressure reducing tower T04, and the heavy component outlet of the recovery tower T05 is communicated with a wastewater discharge pipeline.
The pressure-reduction five-tower four-effect methanol rectification device provided by the utility model mixes crude methanol from a boundary area with alkali liquor and then enters a crude methanol preheater from a main feed pipe, the mixture enters a pre-rectification tower after being preheated to separate light impurities, steam at the top of the pre-rectification tower is condensed and then flows back to the pre-rectification tower, and crude methanol of heavy components at the bottom of the pre-rectification tower enters a pressurizing tower for rectification; condensing methanol gas at the top of the pressurizing tower, sending one part of the condensed methanol gas out as a product, returning the other part of the condensed methanol gas back to the pressurizing tower as reflux, and rectifying heavy component tower bottom materials at the bottom of the pressurizing tower in a normal pressure tower; after the materials at the top of the atmospheric tower are condensed, one part of the condensed materials are sent out as products, the other part of the condensed materials are returned to the atmospheric tower as reflux, and the mixture of the methanol, the water and the mixed alcohol at the bottom of the atmospheric tower is sent to a vacuum tower for further rectification; condensing the top gas of the pressure reducing tower, sending one part of the condensed top gas out as a product, returning the other part of the condensed top gas to the pressure reducing tower as reflux, and sending the methanol-water solution at the bottom of the pressure reducing tower to a recovery tower; and (3) cooling one part of the material steam at the top of the recovery tower, sending the cooled part of the material steam to a mixed alcohol tank, returning the other part of the material steam as reflux to the recovery tower, and sending the qualified wastewater at the bottom of the recovery tower out of the battery limit area through a wastewater discharge pipeline.
As shown in FIG. 1, in a preferred embodiment, crude methanol preheater E01, comprises a flow line in communication with a main feed line and a heat source line; the crude methanol preheater is mainly used for preheating cold material flow crude methanol entering from a main feeding pipeline, and the steam of the three heat source pipelines fully ensures the preheating of the crude methanol in the material flow pipelines.
As shown in fig. 1, in a preferred embodiment, the feed inlet of the pre-rectifying tower T01 is communicated with the crude methanol preheater E01, the pre-rectifying tower T01 comprises a light component outlet and a heavy component outlet, the pre-rectifying tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the pre-rectifying tower T01, and the steam condensate outlet of the heat source pipeline is communicated with the heat source pipeline inlet of the crude methanol preheater E01; the pre-rectifying tower reboiler is divided into a first pre-rectifying tower reboiler E02, a second pre-rectifying tower reboiler E03 and a third pre-rectifying tower reboiler E04; the inlet of a heat source pipeline of the first pre-rectifying tower reboiler E02 is communicated with 0.5MPaG steam of an external heat source, and the steam condensate outlet of the heat source pipeline is communicated with the inlet of a heat source pipeline of a crude methanol preheater E01; an inlet of a heat source pipeline of a second pre-rectifying tower reboiler E03 is communicated with a light component outlet of a recovery tower T05, and a steam condensate outlet of the heat source pipeline is communicated with a reflux tank V05 of the recovery tower; and the inlet of a heat source pipeline of the third pre-rectifying tower reboiler E04 is communicated with the steam condensate outlet of the pressurizing tower reboiler E06, and the steam condensate outlet of the heat source pipeline is communicated with the inlet of a heat source pipeline of the crude methanol preheater E01. The pre-rectifying tower T01 adopts three reboilers which are relatively independent mainly based on heat sources and have different heat source properties, the first pre-rectifying tower reboiler E02 is used as a heat source for 0.5MPaG steam of the steam outside the first pre-rectifying tower reboiler E02, the second pre-rectifying tower reboiler E03 is used for recovering tower top material steam 32 as a heat source, the third pre-rectifying tower reboiler E04 is used for pressurizing tower reboiler steam condensate 17 as a heat source, and the three reboilers can realize flexible load adjustment in a certain range, for example, when the load of the recovering tower is reduced, the stable operation of the pre-rectifying tower can be realized by adjusting the steam quantity of the reboiler E02; the operation pressure at the top of the pre-rectifying tower T01 can be controlled at 150-200KPa.A, and the operation temperature at the top of the pre-rectifying tower can be controlled at 80-90 ℃.
As shown in fig. 1, in a preferred embodiment, the feed inlet of the pressurized column T02 is in communication with the heavy component outlet of the pre-rectification column T01, the pressurized column T02 comprises a light component outlet and a heavy component outlet, the pressurized column reboiler comprises a stream line and a heat source line, the stream line is in communication with the pressurized column T02, and the vapor condensate outlet of the heat source line is in communication with the heat source line inlet of the pre-rectification column reboiler; the feed inlet of the pressurizing tower T02 is communicated with the heavy component outlet of the pre-rectifying tower T01 through a prognostic pump P02, the heavy component of the pre-rectifying tower T01 is pumped into the pressurizing tower T02 through the prognostic pump for further rectification, the light component obtained by rectification in the pressurizing tower T02 flows through a normal pressure tower reboiler E08 and a pressurizing tower reflux tank V02 through the tower top light component outlet and then is shunted through a pressurizing tower reflux pump P03, the first stream is communicated with the pressurizing tower T02, the second stream is communicated with a methanol product collecting part through a pressurizing tower product cooler E07, so that the heat energy can be recycled, the equipment arrangement is more reasonable, the pipeline material consumption of the device is reduced, and the field operation and the operation maintenance are convenient. The inlet of a heat source pipeline of the pressurizing tower reboiler E06 is communicated with external heat source 0.8MPaG steam, and the external steam is used as the heat source to realize the flexible adjustment of the loads of the pressurizing tower and the whole rectifying system; the operation pressure at the top of the pressurizing tower T02 can be controlled at 600-800KPa.A, and the operation temperature at the top of the pressurizing tower T02 can be controlled at 125-135 ℃.
As shown in fig. 1, in a preferred embodiment, the feed inlet of the atmospheric tower T03 is communicated with the heavy component outlet of the pressurized tower T02, the atmospheric tower T03 comprises a light component outlet and a heavy component outlet, the atmospheric tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the atmospheric tower T03, the inlet of the heat source pipeline is communicated with the light component outlet of the pressurized tower T02, and the steam condensate outlet of the heat source pipeline is communicated with the pressurized tower T02 through a pressurized tower reflux tank V02; the feed inlet of the atmospheric tower T03 is communicated with the heavy component outlet of the pressurized tower T02 through a first tower kettle pump P04; light components in the atmospheric tower T03 flow out from a light component outlet at the top of the tower, are communicated with an atmospheric tower reflux tank V03 through a decompression tower reboiler, the atmospheric tower reflux tank V03 is communicated with a pipeline behind a constant pressure tower reflux pump P05, a first stream is communicated with the atmospheric tower T03, a second stream is communicated with a methanol product collecting position through an atmospheric tower product cooler E09, and the consumption of pipeline materials of the device is reduced under the condition of cyclic utilization of heat energy; the operation pressure at the top of the atmospheric tower T03 can be controlled at 150 KPa.A and the operation temperature at the top of the atmospheric tower T03 can be controlled at 75-85 ℃.
As shown in fig. 1, in a preferred embodiment, the feed inlet of the vacuum tower T04 is communicated with the heavy component outlet of the atmospheric tower T03, the vacuum tower T04 comprises a light component outlet and a heavy component outlet, the vacuum tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the vacuum tower T04, the vacuum tower reboiler is divided into a first vacuum tower reboiler E10 and a second vacuum tower reboiler E11, the heat source pipeline of the first vacuum tower reboiler E10 is communicated with the pre-rectifying tower T01, the heat source pipeline of the second vacuum tower reboiler E11 is communicated with the atmospheric tower T03, and the light component outlet of the vacuum tower T04 is communicated with the vacuum tower T04 through the tower top condenser E12 and the vacuum tower reflux tank V04; the feed inlet of the vacuum tower T04 is communicated with the heavy component outlet of the atmospheric tower T03 through a second tower kettle pump P06; the heat source pipeline inlet of the first vacuum tower reboiler E10 is communicated with the light component outlet of the pre-rectifying tower T01, the heat source pipeline steam condensate outlet of the first vacuum tower reboiler E10 is communicated with the pre-rectifying tower T01 through the pre-rectifying tower reflux tank V01, the heat source pipeline inlet of the second vacuum tower reboiler E11 is communicated with the light component outlet of the atmospheric tower T03, and the heat source pipeline steam condensate outlet of the second vacuum tower reboiler E11 is communicated with the atmospheric tower T03 through the atmospheric tower reflux tank V03, so that the loads of the pre-rectifying tower T01 and the atmospheric tower T03 can be adjusted within a certain range to realize flexible adjustment of the load of the vacuum tower T04; the atmospheric tower reflux tank V03 is communicated with an atmospheric tower T03 through an atmospheric tower reflux pump P05; a heat source pipeline steam condensate outlet of the first decompression tower reboiler E10 is communicated with a pre-rectifying tower reflux tank V01 through a pre-rectifying tower top cooler E05, and the pre-rectifying tower reflux tank V01 is communicated with a pre-rectifying tower T01 through a pre-rectifying tower reflux pump P01; a light component outlet of a decompression tower T04 is communicated with a decompression tower (T04) through an overhead condenser E12 and a decompression tower reflux tank V04, the overhead condenser E12 is communicated with a vacuum pump P11 through a vacuum buffer tank V06, the decompression tower reflux tank V04 is divided by a pipeline after passing through a decompression tower reflux pump P07, a first stream is communicated with a decompression tower T04, and a second stream is communicated with a methanol product collection part, so that the heat energy recycling is facilitated, and the on-site operation and operation maintenance are facilitated; the operation pressure of the top/bottom of the vacuum tower T04 can be controlled between 50 KPa.A and 100KPa.A, and the operation temperature of the top of the vacuum tower T04 can be controlled between 50 ℃ and 60 ℃.
As shown in fig. 1, in a preferred embodiment, the feed inlet of the recovery tower T05 is communicated with the heavy component outlet of the vacuum tower T04, the recovery tower T05 comprises a light component outlet and a heavy component outlet, the reboiler of the recovery tower comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the recovery tower T05, the steam condensate outlet of the heat source pipeline is communicated with the heat source pipeline inlet of the crude methanol preheater E01, the light component outlet of the recovery tower T05 is communicated with the heat source pipeline inlet of the reboiler of the pre-rectification tower, the steam condensate outlet of the heat source pipeline of the reboiler of the pre-rectification tower is communicated with the recovery tower T05 through the reflux tank of the recovery tower, and the heavy component outlet of the recovery tower T05 is communicated with the wastewater discharge pipeline; the feed inlet of the recovery tower T05 is communicated with the heavy component outlet of the vacuum tower T04 through a third tower kettle pump P08; the reflux tank V05 of the recovery tower is divided by a pipeline after passing through a reflux pump P09 of the recovery tower, the first stream is communicated with the recovery tower T05, and the second stream is communicated with a mixed alcohol product collecting position through a mixed alcohol product cooler E14; a heavy component outlet of the recovery tower T05 is communicated with a wastewater discharge pipeline through a fourth tower kettle pump P10, a side line is arranged on the recovery tower T05 to extract mixed alcohol, and the organic impurity content in the tower bottom wastewater is further ensured to meet the discharge index requirement; the heat source pipeline inlet of the recovery tower reboiler E13 is communicated with external heat source 0.5MPaG steam; the operation pressure of the top/bottom of the T05 tower can be controlled at 200-300KPa.A, and the operation temperature of the top of the tower can be controlled at 100-110 ℃.
A100-million ton/year methanol rectification device shown in FIG. 1 is adopted: compared with the traditional 3+1 tower device (the steam consumption of each ton of refined methanol product is 1.25 tons, the circulating water consumption is 75 tons), the operating cost can be saved by 7690 ten thousand yuan RMB each year, the economic benefit is remarkable, and the specific characteristics are as follows:
the steam cost: (1.25-0.78) 150 × 100 ten thousand tons/year 7050 ten thousand yuan.
The cost of circulating water: (75-43) 0.2 100 ten thousand tons/year 640 ten thousand yuan
Thirdly, in total: 7050 ten thousand yuan +640 ten thousand yuan 7690 ten thousand yuan
Compared with the device shown in the figure 1, the height of a recovery tower T05 of a 100 ten thousand ton/year methanol rectification device is reduced, the quality requirement of the material at the top of the recovery tower T05 is reduced, and the product at the top of the tower is used as fuel oil to be supplied to a steam superheater or an incinerator in a factory, so that the device can reduce the steam consumption at the bottom of the recovery tower and save the operation cost; the equipment investment of the recovery tower T05 can be reduced by 25 ten thousand yuan, the steam consumption of each ton of refined methanol products is 0.75 ton, the circulating water consumption is 43 tons, the steam price is 150 yuan/ton, and the circulating water price is 0.2 yuan/ton, compared with the traditional 3+1 tower device, the recovery tower T05 can save the running cost of 8140 thousand yuan RMB each year, the economic benefit is obvious, and the recovery tower T05 is specifically as follows:
the steam cost: (1.25-0.75) 150 × 100 ten thousand tons/year 7500 ten thousand yuan.
The cost of circulating water: (75-43) 0.2 100 ten thousand tons/year 640 ten thousand yuan
Thirdly, in total: 7500 ten thousand yuan +640 ten thousand yuan is 8140 ten thousand yuan
Compared with the device shown in the figure 1, the device shown in the figure 2 is additionally provided with a reboiler E15, and the heat is supplied by adopting the waste heat of materials, so that the required heat level is not high and the waste heat of other device materials (such as the synthesis gas of a methanol synthesis device) in a plant can be met by considering that the operation pressure at the top of the pre-rectifying tower T01 is 150-200 KPa.A., the operation temperature at the top of the pre-rectifying tower is 80-90 ℃, and the device can further reduce the steam consumption of a steam heater E02. A 100-million ton/year methanol rectification device shown in fig. 2 was used: the steam consumption of each ton of refined methanol products is 0.57 ton, the circulating water consumption is 43 ton, the steam price is 150 yuan/ton, the circulating water price is 0.2 yuan/ton, compared with the traditional 3+1 tower device, the operating cost can be saved by 10840 yuan of renminty money every year, the economic benefit is remarkable, and the method specifically comprises the following steps:
the steam cost: (1.25-0.57) 150 × 100 ten thousand tons/year 10200ten thousand yuan.
The cost of circulating water: (75-43) 0.2 100 ten thousand tons/year 640 ten thousand yuan
Thirdly, in total: 10200 ten thousand yuan +640 ten thousand yuan 10840 ten thousand yuan
In conclusion, when the pressure-reduction type five-tower four-effect methanol rectifying device provided by the utility model is used for rectifying methanol, the device has high operation stability and low energy consumption, and the operation cost is greatly reduced, so that the pressure-reduction type five-tower four-effect methanol rectifying device effectively overcomes various defects in the prior art and has high industrial utilization value.
The foregoing embodiments are merely illustrative of the principles and utilities of the present invention and are not intended to limit the utility model. Any person skilled in the art can modify or change the above-mentioned embodiments without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which can be made by those skilled in the art without departing from the spirit and technical spirit of the present invention be covered by the claims of the present invention.
Claims (10)
1. The utility model provides a decompression type five tower four-effect methyl alcohol rectifier unit which characterized in that, the device includes: a crude methanol preheater (E01), a pre-rectifying tower (T01) and a pre-rectifying tower reboiler, a pressurized tower (T02) and a pressurized tower reboiler, an atmospheric tower (T03) and an atmospheric tower reboiler, a vacuum tower (T04) and a vacuum tower reboiler, a recovery tower (T05) and a recovery tower reboiler; wherein: the crude methanol preheater (E01) is communicated with a total feeding pipeline, the feed inlet of a pre-rectifying tower (T01) is communicated with the crude methanol preheater (E01), the feed inlet of a pressurizing tower (T02) is communicated with the heavy component outlet of the pre-rectifying tower (T01), the feed inlet of an atmospheric tower (T03) is communicated with the heavy component outlet of the pressurizing tower (T02), the feed inlet of a pressure reducing tower (T04) is communicated with the heavy component outlet of the atmospheric tower (T03), the feed inlet of a recovery tower (T05) is communicated with the heavy component outlet of the pressure reducing tower (T04), and the heavy component outlet of the recovery tower (T05) is communicated with a wastewater discharge pipeline.
2. The reduced-pressure five-tower four-effect methanol rectification device according to claim 1, characterized in that the crude methanol preheater (E01) comprises a material flow pipeline and a heat source pipeline, wherein the material flow pipeline is communicated with a total feeding pipeline;
the pre-rectifying tower (T01) comprises a light component outlet and a heavy component outlet, the pre-rectifying tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the pre-rectifying tower (T01), and a steam condensate outlet of the heat source pipeline is communicated with a heat source pipeline inlet of the crude methanol preheater (E01);
the pressurized tower (T02) and a pressurized tower reboiler, wherein the pressurized tower (T02) comprises a light component outlet and a heavy component outlet, the pressurized tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the pressurized tower (T02), and a steam condensate outlet of the heat source pipeline is communicated with a heat source pipeline inlet of the pre-rectifying tower reboiler;
in the atmospheric tower (T03) and an atmospheric tower reboiler, the atmospheric tower (T03) comprises a light component outlet and a heavy component outlet, the atmospheric tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the atmospheric tower (T03), an inlet of the heat source pipeline is communicated with the light component outlet of the pressurized tower (T02), and a steam condensate outlet of the heat source pipeline is communicated with the pressurized tower (T02) through a pressurized tower reflux tank (V02);
in the vacuum column (T04) and the vacuum column reboiler, the vacuum column (T04) comprises a light component outlet and a heavy component outlet, the pressure reducing tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the pressure reducing tower (T04), the vacuum tower reboiler is divided into a first vacuum tower reboiler (E10) and a second vacuum tower reboiler (E11), the heat source pipeline of the first decompression column reboiler (E10) is communicated with the pre-rectifying column (T01), the heat source pipeline of the second vacuum tower reboiler (E11) is communicated with the atmospheric tower (T03), the steam condensate outlet of the heat source pipeline of the second vacuum tower reboiler (E11) is communicated with the atmospheric tower (T03) through an atmospheric tower reflux tank (V03), the light component outlet of the vacuum tower (T04) is communicated with the vacuum tower (T04) through an overhead condenser (E12) and a vacuum tower reflux tank (V04);
in the recovery tower (T05) and the recovery tower reboiler, the recovery tower (T05) comprises a light component outlet and a heavy component outlet, the recovery tower reboiler comprises a material flow pipeline and a heat source pipeline, the material flow pipeline is communicated with the recovery tower (T05), a steam condensate outlet of the heat source pipeline is communicated with a heat source pipeline inlet of the crude methanol preheater (E01), a light component outlet of the recovery tower (T05) is communicated with a heat source pipeline inlet of the pre-rectifying tower reboiler, and a heat source pipeline steam condensate outlet of the pre-rectifying tower reboiler is communicated with the recovery tower (T05) through a recovery tower reflux tank (V05).
3. The reduced-pressure five-tower four-effect methanol rectification device according to claim 1, characterized in that the feed inlet of the pressurized tower (T02) is communicated with the heavy component outlet of the pre-rectification tower (T01) through a pre-pump (P02);
and/or the feed inlet of the atmospheric tower (T03) is communicated with the heavy component outlet of the pressurized tower (T02) through a first tower kettle pump (P04);
and/or the feed inlet of the vacuum tower (T04) is communicated with the heavy component outlet of the atmospheric tower (T03) through a second tower kettle pump (P06);
and/or the feed inlet of the recovery column (T05) is communicated with the heavy component outlet of the decompression column (T04) through a third column kettle pump (P08);
and/or the heavy component outlet of the recovery tower (T05) is communicated with the waste water discharge pipeline through a fourth tower kettle pump (P10).
4. The reduced-pressure five-tower four-effect methanol rectification device according to claim 2, wherein the pre-rectifying tower reboiler comprises a first pre-rectifying tower reboiler (E02), a second pre-rectifying tower reboiler (E03) and a third pre-rectifying tower reboiler (E04), the vapor condensate outlet of the heat source pipeline of the first pre-rectifying tower reboiler (E02) is communicated with the heat source pipeline inlet of the crude methanol preheater (E01), the heat source pipeline inlet of the second pre-rectifying tower reboiler (E03) is communicated with the light component outlet of the recovery tower (T05), and the vapor condensate outlet of the heat source pipeline of the third pre-rectifying tower reboiler (E04) is communicated with the heat source pipeline inlet of the crude methanol preheater (E01).
5. The pressure-reduced five-tower four-effect methanol rectification device according to claim 2, characterized in that the pressure tower reflux tank (V02) is branched by a pressure tower reflux pump (P03) and a pipeline, the first stream is communicated with the pressure tower (T02), and the second stream is communicated with a methanol product collecting place by a pressure tower product cooler (E07).
6. The vacuum type five-tower four-effect methanol rectification device according to claim 2, characterized in that the atmospheric tower reflux tank (V03) is branched by a pipeline after passing through an atmospheric tower reflux pump (P05), the first stream is communicated with the atmospheric tower (T03), and the second stream is communicated with a methanol product collecting place through an atmospheric tower product cooler (E09).
7. The reduced-pressure five-tower four-effect methanol rectification device according to claim 2, characterized in that a heat source pipeline inlet of the first reduced-pressure tower reboiler (E10) is communicated with a light component outlet of the pre-rectifying tower (T01), a heat source pipeline steam condensate outlet of the first reduced-pressure tower reboiler (E10) is communicated with the pre-rectifying tower (T01) through a pre-rectifying tower reflux tank (V01), and a heat source pipeline inlet of the second reduced-pressure tower reboiler (E11) is communicated with a light component outlet of the atmospheric tower (T03);
and/or a heat source pipeline steam condensate outlet of the first decompression tower reboiler (E10) is communicated with a pre-rectifying tower reflux tank (V01) through a pre-rectifying tower top cooler (E05), and the pre-rectifying tower reflux tank (V01) is communicated with the pre-rectifying tower (T01) through a pre-rectifying tower reflux pump (P01).
8. The reduced-pressure five-tower four-effect methanol rectification plant according to claim 2, characterized in that the vent outlet of the overhead condenser (E12) is communicated with the vacuum pump (P11) through a vacuum buffer tank (V06) by an air exhaust line (28).
9. The decompression type five-tower four-effect methanol rectification device according to claim 2, wherein the decompression tower reflux tank (V04) is branched by a pipeline after a decompression tower reflux pump (P07), the first stream is communicated with the decompression tower (T04), and the second stream is communicated with a methanol product collecting place.
10. The vacuum type five-tower four-effect methanol rectification device according to claim 2, characterized in that the recovery tower reflux tank (V05) is branched by a pipeline after a recovery tower reflux pump (P09), the first stream is communicated with the recovery tower (T05), and the second stream is communicated with a mixed alcohol product collecting place through a mixed alcohol product cooler (E14).
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| CN202121779130.1U CN216404258U (en) | 2021-08-02 | 2021-08-02 | Decompression type five-tower four-effect methanol rectification device |
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