Comprehensive utilization device for byproduct fusel oil of ethylene glycol co-production methanol device

Abstract

The utility model provides a comprehensive utilization device for a byproduct fusel oil of an ethylene glycol co-production methanol device, and relates to the technical field of ethylene glycol co-production methanol. Comprising a methanol rectification separation device, an ethylene glycol rectification separation device, a membrane separation device and a penetrating fluid treatment device, an outlet of the methanol rectification separation device is connected with an inlet of the ethylene glycol rectification separation device, and an outlet of the ethylene glycol rectification separation device is connected with an inlet of the membrane separation device; and the outlet of the membrane separation device is connected with the inlet of the penetrating fluid treatment device. According to the technical improvement project, fusel oil raw materials come from an ethylene glycol rectification system and a methanol rectification system, the fusel oil raw materials and a main production system are started and stopped at the same time, a newly-added fusel oil recovery device frame and an existing methanol rectification system are connected into a whole and are regarded as a set of device, namely, existing device public engineering is fully relied on, and the production cost is reduced. The method has the advantages of short flow, complete supporting facilities, low investment and the like.

Description

Technical Field

[0001] The utility model relates to the technical field of ethylene glycol co-production of methanol, in particular to a device for comprehensively utilizing fusel oil, a byproduct of an ethylene glycol co-production of methanol device. Background Art

[0002] In the prior art, the ethylene glycol distillation system adopts a five-tower process, namely, a methanol recovery tower, a dehydration tower, a dealcoholization tower, an ethylene glycol product tower, and an ethylene glycol recovery tower. Among them, in the dehydration tower, after the crude ethylene glycol from the methanol recovery tower is separated, the top gas phase is a vapor containing light components such as C2-C5 alcohols, methyl glycolate, and dimethyl oxalate. After condensation in the dehydration tower condenser, the liquid phase enters the dehydration tower reflux tank, most of which returns to the dehydration tower as reflux liquid, and a small amount of produced liquid is sent to the fusel oil storage tank. The methanol distillation system adopts a three-tower distillation process, namely, a pre-tower, a pressure tower, and an atmospheric pressure tower. Among them, a large amount of by-product isobutyl oil accumulates in the middle and lower part of the atmospheric tower. If it cannot be extracted in time, it will inevitably affect the quality of the refined methanol product extracted from the top of the atmospheric tower. There is a fusel oil extraction outlet at the lower part of the atmospheric tower. During operation, combined with the production situation, it is generally extracted continuously and enters the isobutyl oil storage tank. The main components are methanol, ethanol, water, etc., and finally sent to the fusel oil storage tank in the tank area. Finally, it is sold as crude methanol at a price of only 500 yuan / ton.

[0003] The fusel oil extracted from the dehydration tower of the ethylene glycol distillation system contains a large amount of methanol and ethanol. At present, Zhongyan Hongsifang sells it as fusel oil at a relatively low market price. Compared with other components in fusel oil, methanol has a relatively low boiling point and can be recovered by ordinary distillation; while for the separation of ethanol-water azeotropes, extractive distillation and salt distillation processes are generally used in industry. Therefore, the development of a recovery process for fusel oil in the dehydration tower can not only meet the requirements of green development, but also obtain high-purity by-products, bringing considerable economic benefits to the production process.

[0004] In order to ensure the quality of refined methanol products, the methanol distillation system needs to produce a large amount of fusel oil (isobutyl oil). However, this fusel oil has a complex composition and is difficult to sell. As the production time of the system increases, the storage volume of fusel oil becomes larger and larger, becoming a hidden worry and burden for production.

[0005] At present, the domestic use of intermittent evaporation recovery and continuous distillation recovery methods for fusel oil in methanol distillation system is generally adopted. The obtained refined methanol still contains a lot of impurities, which is generally not mixed with the refined methanol extracted from the main tower, and can only be sold or used as a low-grade methanol product; in both intermittent evaporation recovery and continuous distillation recovery processes, there is a very small amount of evaporation residue with high impurity content that needs to be discharged, and there is a problem of secondary waste treatment. Since the boiling points of methanol and ethanol in the fusel oil of methanol distillation system are close, it is also quite difficult to carry out distillation treatment, and there is no special or good treatment method. Some manufacturers also have to adopt incineration to dispose of fusel oil in methanol distillation system, because fusel oil contains high value-added alcohols, and incineration treatment will cause waste of resources. This urgently needs to find a way to recycle and utilize fusel oil in methanol distillation system with low treatment cost. Utility Model Content

[0006] 1. Technical issues to be resolved

[0007] In view of the deficiencies of the prior art, the utility model provides a device for comprehensively utilizing the by-product fusel oil of an ethylene glycol co-production methanol device, which solves the technical problem that the prior art cannot recycle the fusel oil of a methanol distillation system and has a low treatment cost.

[0008] (II) Technical solution

[0009] In order to achieve the above objectives, the present invention is implemented through the following technical solutions:

[0010] The utility model solves the technical problem and provides a device for comprehensively utilizing fusel oil, a byproduct of an ethylene glycol co-production methanol device, comprising a methanol distillation and separation device, an ethylene glycol distillation and separation device, a membrane separation device and a permeate treatment device; the outlet of the methanol distillation and separation device is connected to the inlet of the ethylene glycol distillation and separation device; the outlet of the ethylene glycol distillation and separation device is connected to the inlet of the membrane separation device; the outlet of the membrane separation device is connected to the inlet of the permeate treatment device; the methanol distillation and separation device comprises a raw material buffer tank, a de-methanol tower feed pump group, a wastewater preheater, a condensate preheater, a de-methanol tower, a de-methanol tower top condenser, a de-methanol tower top reflux tank, a de-methanol tower top reflux pump group, a de-methanol tower top cooler, and a methanol recovery device. The intermediate tank and the de-methanol tower kettle pump group; the raw material buffer tank is connected with the feed port in the middle of the de-methanol tower through the wastewater preheater and the condensate preheater in turn, and the conveying power is provided by the de-methanol tower feed pump group; the upper part of the de-methanol tower is provided with a de-methanol tower top condenser; the de-methanol tower top condenser is connected with the inlet of the de-methanol tower top reflux tank; the outlet of the de-methanol tower top reflux tank is connected with the feed port at the top of the de-methanol tower and the conveying power is provided by the de-methanol tower top reflux pump group; the outlet of the de-methanol tower top reflux tank is connected with the feed port of the methanol recovery intermediate tank through the de-methanol tower top cooler and the conveying power is provided by the de-methanol tower top reflux pump group; the ethylene glycol distillation separation device includes a de-ethanol tower, a de-ethanol tower top condenser, A deethanol tower top reflux tank, a deethanol tower top reflux pump group, a deethanol tower top cooler, an ethanol distillate receiving tank, a deethanol tower kettle pump group, a wastewater cooler and a coal slurry gasification section device; the feed inlet in the middle of the deethanol tower is connected to the kettle of the demethanol tower and the conveying power is provided by the demethanol tower kettle pump group; a deethanol tower top condenser is arranged on the upper part of the deethanol tower; the deethanol tower top condenser is connected to the inlet of the deethanol tower top reflux tank; the outlet of the deethanol tower top reflux tank is connected to the feed inlet of the deethanol tower top and the conveying power is provided by the deethanol tower top reflux pump group; the outlet of the deethanol tower top reflux tank is connected to the feed inlet of the ethanol distillate receiving tank through the deethanol tower top cooler and the conveying power is provided by the deethanol tower top reflux pump group Supplying conveying power; the kettle of the deethanol tower is connected with the coal slurry gasification section device through the wastewater preheater and the wastewater cooler in turn, and the conveying power is provided by the deethanol tower kettle pump group; the membrane separation device includes a membrane feed pump group, a membrane preheater, a membrane evaporator, a superheater 1, a membrane separation unit, a finished product condenser, a membrane finished product tank, a membrane finished product pump group and an ethanol finished product intermediate tank; the discharge port of the ethanol distillate receiving tank is connected with the inlet of the membrane evaporator through the membrane preheater and the conveying power is provided by the membrane feed pump group; the outlet of the membrane evaporator is connected with the inlet of the membrane separation unit through the superheater 1; the outlet of the membrane separation unit is connected with the inlet of the finished product condenser through the membrane preheater; the outlet of the finished product condenser is connected with the inlet of the membrane finished product tank;The outlet of the finished membrane tank is connected to the inlet of the ethanol finished intermediate tank and is powered by the finished membrane pump group; the outlet of the finished membrane tank is connected to the inlet of the ethanol distillate receiving tank and is powered by the finished membrane pump group; the outlet of the finished membrane tank is connected to the inlet of the ethanol finished intermediate tank and is powered by the finished membrane pump group; the permeate treatment device includes a permeate condenser unit, a vacuum unit, a tail gas condenser, a tail gas tank and a tail gas pump; the permeate condenser unit is connected to the membrane separation unit; the permeate condenser unit is connected to the air inlet of the vacuum unit; the exhaust port of the vacuum unit is provided with a tail gas condenser; the tail gas condenser is connected to the feed port of the tail gas tank; the discharge port of the tail gas tank is connected to the raw material buffer tank and is powered by the tail gas pump. ;

[0011] Furthermore, the membrane separation unit includes membrane assembly one, membrane assembly two, membrane assembly three, membrane assembly four, superheater two, superheater three and superheater four; the inlet of membrane assembly one is connected to superheater one, and superheater two is arranged between the mixed alcohol outlet of membrane assembly one and the inlet of membrane assembly two; superheater three is arranged between the mixed alcohol outlet of membrane assembly two and the inlet of membrane assembly three; superheater four is arranged between the mixed alcohol outlet of membrane assembly three and the inlet of membrane assembly four; the mixed alcohol outlet of membrane assembly four is connected to the membrane preheater.

[0012] Furthermore, the permeate condenser unit includes a permeate condenser 1 and a permeate condenser 2; the inlet of the permeate condenser 1 is connected to the permeate outlet of membrane assembly 1 and the permeate outlet of membrane assembly 2; the inlet of the permeate condenser 2 is connected to the permeate outlet of membrane assembly 3 and the permeate outlet of membrane assembly 4; the outlet of the permeate condenser 1 is connected to the inlet of the permeate condenser 2.

[0013] Furthermore, the permeate treatment device also includes a permeate tank; the permeate outlet of the permeate condenser 1 and the permeate outlet of the permeate condenser 2 are both connected to the feed inlet of the permeate tank.

[0014] Furthermore, the permeate treatment device also includes a permeate pump and a wastewater treatment device; the discharge port of the permeate tank is connected to the wastewater treatment device and the permeate pump provides the conveying power.

[0015] Furthermore, the vacuum unit includes vacuum machine 1 and vacuum machine 2; the air inlet of vacuum machine 1 is connected to the outlet of permeate condenser 2; the exhaust port of vacuum machine 1 is connected to the air inlet of vacuum machine 2; the exhaust port of vacuum machine 2 is connected to the exhaust gas condenser.

[0016] Furthermore, the methanol distillation separation device also includes a de-methanol tower reboiler; the de-methanol tower reboiler is arranged at the lower part of the de-methanol tower.

[0017] Furthermore, the de-methanol tower reboiler is configured as a thermal siphon reboiler; the de-methanol tower reboiler adopts 0.5MPaG saturated steam for heating and gasification.

[0018] Furthermore, the ethylene glycol distillation separation device also includes a deethanol tower reboiler; the deethanol tower reboiler is arranged at the lower part of the deethanol tower.

[0019] Furthermore, the deethanol tower reboiler is configured as a thermal siphon reboiler; the deethanol tower reboiler adopts 0.5MPaG saturated steam for heating and gasification.

[0020] (III) Beneficial effects

[0021] 1. The fusel oil raw materials of the technical transformation project of the utility model come from the ethylene glycol distillation system and the methanol distillation system, which are operated at the same time as the main production system. The newly added fusel oil recovery device framework and the existing methanol distillation system are integrated into one, which is regarded as a set of devices, that is, it fully relies on the public engineering of the existing device, and has the advantages of short process, complete supporting facilities and small investment.

[0022] 2. The utility model adopts double-effect distillation heat coupling technology - rationally utilizes the waste heat of the extracted materials to heat the feed, optimizes the heat exchange network, and can effectively reduce the energy consumption of the distillation process. The heat of the feed of the deethanol tower is recycled to improve the energy utilization efficiency and reduce the energy consumption of the system.

[0023] 3. In the fusel oil system of the utility model, ethanol and water will form a minimum azeotrope under normal pressure, which is difficult to separate. Through systematic analysis of the separation effect of the materials in the deethanol tower, high-efficiency tower internals are used to replace the traditional method of using an extractant; at the same time, the purpose of energy saving and consumption reduction and improving economic benefits can be achieved.

[0024] 4. The utility model adopts membrane technology to dehydrate ethanol, which solves the problem of large floor space and inability to handle waste solids in traditional molecular sieve dehydration.

[0025] 5. The utility model utilizes the existing facilities in the factory area to make full use of the alcohol-ester mixture in the wastewater, and uses the wastewater gasification pulping system as pulping water replenishment, which can effectively solve the environmental protection problem. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0027] Figure 1 It is a structural schematic diagram of a methanol distillation and separation device connected to an ethylene glycol distillation and separation device in a device for comprehensive utilization of by-product fusel oil of an ethylene glycol co-production methanol device in the utility model;

[0028] Figure 2 It is a structural schematic diagram of a membrane separation device and a permeate treatment device connected to a device for comprehensive utilization of fusel oil by-product of an ethylene glycol co-production methanol device in the utility model;

[0029] In the accompanying drawings, the components represented by the reference numerals are listed as follows:

[0030] 1-raw material buffer tank, 2-de-methanol tower feed pump group, 3-wastewater preheater, 4-condensate preheater, 5-de-methanol tower, 6-de-methanol tower top condenser, 7-de-methanol tower top reflux tank, 8-de-methanol tower top reflux pump group, 9-de-methanol tower top cooler, 10-methanol recovery intermediate tank, 11-de-methanol tower bottom pump group, 12-de-ethanol tower, 13-de-ethanol tower top condenser, 14-de-ethanol tower top reflux tank, 15-de-ethanol tower top reflux pump group, 16-de-ethanol tower top cooler, 17-ethanol distillate receiving tank, 18-de-ethanol tower bottom pump group, 19-wastewater cooler, 20-coal slurry gasification section device, 21-membrane feed pump group, 22-membrane Preheater, 23-membrane evaporator, 24-superheater 1, 25-finished product condenser, 26-membrane finished product tank, 27-membrane finished product pump group, 28-ethanol finished product intermediate tank, 29-tail gas condenser, 30-tail gas liquid tank, 31-tail gas liquid pump, 32-membrane assembly 1, 33-membrane assembly 2, 34-membrane assembly 3, 35-membrane assembly 4, 36-superheater 2, 37-superheater 3, 38-superheater 4, 39-permeate condenser 1, 40-permeate condenser 2, 41-permeate tank, 42-permeate pump, 43-wastewater treatment device, 44-vacuum machine 1, 45-vacuum machine 2, 46-methanol removal tower reboiler, 47-ethanol removal tower reboiler. DETAILED DESCRIPTION

[0031] In order to make the purpose, technical solution and advantages of the embodiments of the utility model clearer, the technical solution in the embodiments of the utility model is described clearly and completely. Obviously, the described embodiments are part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments of the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

[0032] The embodiment of the present application provides a device for comprehensively utilizing fusel oil, a by-product of an ethylene glycol co-production of methanol, thereby solving the technical problem that the prior art cannot recycle fusel oil from a methanol distillation system and has a low treatment cost.

[0033] like Figure 1 to Figure 2 As shown,

[0034] The utility model provides a device for comprehensively utilizing fusel oil, a byproduct of an ethylene glycol co-production of methanol, comprising a methanol distillation and separation device, an ethylene glycol distillation and separation device, a membrane separation device and a permeate treatment device.

[0035] The outlet of the methanol distillation separation device is connected to the inlet of the ethylene glycol distillation separation device, the outlet of the ethylene glycol distillation separation device is connected to the inlet of the membrane separation device, and the outlet of the membrane separation device is connected to the inlet of the permeate treatment device.

[0036] The methanol distillation separation device includes a raw material buffer tank 1, a de-methanol tower feed pump group 2, a wastewater preheater 3, a condensate preheater 4, a de-methanol tower 5, a de-methanol tower top condenser 6, a de-methanol tower top reflux tank 7, a de-methanol tower top reflux pump group 8, a de-methanol tower top cooler 9, a methanol recovery intermediate tank 10 and a de-methanol tower kettle pump group 11.

[0037] The de-methanol tower 5 is operated at normal pressure, and the internal parts are designed with high-performance wire mesh corrugated packing. The raw material buffer tank 1 is connected to the feed port in the middle of the de-methanol tower 5 through the wastewater preheater 3 and the condensate preheater 4 in sequence, and the de-methanol tower feed pump group 2 provides the conveying power.

[0038] A demethanol tower top condenser 6 is provided at the top of the demethanol tower 5, and the demethanol tower top condenser 6 is connected to the inlet of the demethanol tower top reflux tank 7. The outlet of the demethanol tower top reflux tank 7 is connected to the feed port at the top of the demethanol tower 5 and is provided with a conveying power by a demethanol tower top reflux pump group 8. The outlet of the demethanol tower top reflux tank 7 is connected to the feed port of the methanol recovery intermediate tank 10 through a demethanol tower top cooler 9 and is provided with a conveying power by a demethanol tower top reflux pump group 8.

[0039] The ethylene glycol distillation separation device includes a deethanol tower 12, a deethanol tower top condenser 13, a deethanol tower top reflux tank 14, a deethanol tower top reflux pump group 15, a deethanol tower top cooler 16, an ethanol distillate receiving tank 17, a deethanol tower kettle pump group 18, a wastewater cooler 19 and a coal slurry gasification section device 20.

[0040] The feed inlet in the middle of the deethanol tower 12 is connected to the tower kettle of the deethanol tower 5 and is powered by the deethanol tower kettle pump group 11. A deethanol tower top condenser 13 is provided on the upper part of the deethanol tower 12. The deethanol tower top condenser 13 is connected to the inlet of the deethanol tower top reflux tank 14, and the outlet of the deethanol tower top reflux tank 14 is connected to the feed inlet at the top of the deethanol tower 13 and is powered by the deethanol tower top reflux pump group 15.

[0041] The outlet of the deethanol tower top reflux tank 14 is connected to the feed port of the ethanol distillate receiving tank 17 through the deethanol tower top cooler 16, and the conveying power is provided by the deethanol tower top reflux pump group 15. The tower bottom of the deethanol tower 12 is connected to the coal slurry gasification section device 20 through the wastewater preheater 3 and the wastewater cooler 19 in turn, and the conveying power is provided by the deethanol tower bottom pump group 18.

[0042] The membrane separation device includes a membrane feed pump group 21, a membrane preheater 22, a membrane evaporator 23, a superheater 24, a membrane separation unit, a finished product condenser 25, a membrane finished product tank 26, a membrane finished product pump group 27 and an ethanol finished product intermediate tank 28.

[0043] The discharge port of the ethanol distillate receiving tank 17 is connected to the inlet of the membrane evaporator 23 through the membrane preheater 22 and the conveying power is provided by the membrane feed pump group 21. The outlet of the membrane evaporator 23 is connected to the inlet of the membrane separation unit through the superheater 24. The outlet of the membrane separation unit is connected to the inlet of the finished product condenser 25 through the membrane preheater 22.

[0044] The outlet of the finished product condenser 25 is connected to the inlet of the membrane finished product tank 26. The outlet of the membrane finished product tank 26 is connected to the inlet of the ethanol finished product intermediate tank 28 and the membrane finished product pump group 27 provides the conveying power.

[0045] The outlet of the membrane finished product tank 26 is connected to the inlet of the ethanol distillate receiving tank 17 and is powered by the membrane finished product pump group 27. The outlet of the membrane finished product tank 26 is connected to the inlet of the ethanol finished product intermediate tank 28 and is powered by the membrane finished product pump group 27.

[0046] The permeate treatment device includes a permeate condenser unit, a vacuum unit, a tail gas condenser 29 , a tail gas liquid tank 30 and a tail gas liquid pump 31 .

[0047] The permeate condenser unit is connected to the membrane separation unit. The permeate condenser unit is connected to the air inlet of the vacuum unit. The exhaust port of the vacuum unit is provided with a tail gas condenser 29, and the tail gas condenser 29 is connected to the feed port of the tail gas liquid tank 30. The discharge port of the tail gas liquid tank 30 is connected to the raw material buffer tank 1 and the tail gas liquid pump 31 provides the conveying power.

[0048] Specifically, the membrane separation unit includes membrane assembly 1 32, membrane assembly 2 33, membrane assembly 3 34, membrane assembly 4 35, superheater 2 36, superheater 3 37 and superheater 4 38. The inlet of membrane assembly 1 32 is connected to superheater 1 24, superheater 2 36 is arranged between the mixed alcohol outlet of membrane assembly 1 32 and the inlet of membrane assembly 2 33, superheater 3 37 is arranged between the mixed alcohol outlet of membrane assembly 2 33 and the inlet of membrane assembly 3 34, superheater 4 38 is arranged between the mixed alcohol outlet of membrane assembly 3 34 and the inlet of membrane assembly 4 35, and the mixed alcohol outlet of membrane assembly 4 34 is connected to membrane preheater 22.

[0049] Specifically, the permeate condenser unit includes a permeate condenser 39 and a permeate condenser 40. The inlet of the permeate condenser 39 is connected to the permeate outlet of the membrane assembly 1 32 and the permeate outlet of the membrane assembly 2 33. The inlet of the permeate condenser 2 40 is connected to the permeate outlet of the membrane assembly 34 and the permeate outlet of the membrane assembly 4 35. The outlet of the permeate condenser 39 is connected to the inlet of the permeate condenser 2 40.

[0050] Specifically, the permeate processing device further includes a permeate tank 41 , and the permeate outlet of the permeate condenser 1 39 and the permeate outlet of the permeate condenser 2 40 are both connected to the feed port of the permeate tank 41 .

[0051] Specifically, the permeate treatment device further includes a permeate pump 42 and a wastewater treatment device 43 . The discharge port of the permeate tank 41 is connected to the wastewater treatment device 43 and the permeate pump 42 provides the transport power.

[0052] Specifically, the vacuum unit includes a vacuum machine 1 44 and a vacuum machine 2 45 , the air inlet of the vacuum machine 1 44 is connected to the outlet of the permeate condenser 2 40 , the exhaust port of the vacuum machine 1 44 is connected to the air inlet of the vacuum machine 2 45 , and the exhaust port of the vacuum machine 2 45 is connected to the tail gas condenser 29 .

[0053] Preferably, the methanol distillation separation device further includes a de-methanol tower reboiler 46 , and the lower part of the de-methanol tower 5 is provided with the de-methanol tower reboiler 46 .

[0054] Specifically, the de-methanol tower reboiler 46 is configured as a thermal syphon reboiler, and the de-methanol tower reboiler 46 uses 0.5 MPaG saturated steam for heating and gasification.

[0055] Preferably, the ethylene glycol distillation separation device further comprises a deethanol tower reboiler 47 , and the deethanol tower reboiler 47 is disposed at the lower portion of the deethanol tower 12 .

[0056] Specifically, the deethanol tower reboiler 47 is configured as a thermal syphon reboiler, and the deethanol tower reboiler 47 uses 0.5 MPaG saturated steam for heating and gasification.

[0057]

[0058]

[0059]

[0060] List of transmission equipment in the embodiment of the utility model

[0061]

[0062]

[0063] Raw material standards of the utility model embodiment:

[0064] Raw material design components:

[0065] Material Name Methanol Ethanol Alcohol ester water total Composition (wt%) 50±8 10±3 5±2 28±3 100

[0066] Product standards of the utility model embodiment

[0067] Methanol product: methanol purity ≥ 99.0%, water content ≤ 0.03wt.%.

[0068] Ethanol products: Ethanol purity ≥ 99.5%, meeting the first-class standard of 99.5% ethanol in "GB / T6820-2016 Industrial Ethanol".

[0069]

[0070]

[0071] Working principle and use process of the embodiment of the utility model:

[0072] The first step: the fusel oil from the top of the existing dehydration tower of the ethylene glycol unit and the isobutyl oil from methanol are collected in the raw material buffer tank 1, transported by the de-methanol tower feed pump group 2, and sequentially passed through the wastewater preheater 3 and the condensate preheater 4, respectively preheated with the wastewater at the bottom of the de-ethanol tower 12 and the steam condensate of the section, and then enter the middle of the de-methanol tower 5. The de-methanol tower reboiler 46 adopts 0.5MPaG saturated steam for heating and gasification. The methanol vapor that meets the recovery requirements is extracted from the top of the de-methanol tower 5 and condensed by the de-methanol tower top condenser 6. The condensate flows by gravity to the de-methanol tower top reflux tank 7. Part of it is sent to the top of the de-methanol tower 5 as reflux through the de-methanol tower top reflux pump group 8, and the rest is sent to the de-methanol tower top cooler 9 for cooling, and then sent to the methanol recovery intermediate tank 10 as a methanol by-product.

[0073] Step 2: The bottom liquid of the methanol removal tower 5 is transported by the methanol removal tower bottom pump group 11 and then sent to the middle part of the ethanol removal tower 12. The ethanol removal tower reboiler 47 is heated by 0.5MPaG saturated steam. The top of the ethanol removal tower 12 produces ~90% ethanol vapor, which is condensed by the ethanol removal tower top condenser 13. The condensate flows into the ethanol removal tower top reflux tank 14, and is partially sent to the top of the ethanol removal tower 12 for reflux through the ethanol removal tower top reflux pump group 15. The rest is produced to the ethanol distillate receiving tank 17 for dehydration treatment by the subsequent ethanol membrane system. The bottom wastewater is transported by the ethanol removal tower bottom pump group 18, and after heat exchange in the wastewater preheater 3, it is cooled by the wastewater cooler 19 and then sent to the coal slurry gasification section device 20.

[0074] Step 3: The ethanol distillate in the ethanol distillate receiving tank 17 that meets the membrane entry requirements is transported by the membrane feed pump group 21, and enters the membrane evaporator 23 after heat exchange with the ethanol dehydration product in the membrane preheater 22. The water-containing ethanol vapor at the outlet of the membrane evaporator 23 enters the superheater 24 for overheating, and enters the membrane separation unit in the form of superheated steam. The operating pressure of the entire set of membrane separation unit is about 0.2-0.35MPa (G). The membrane separation unit is composed of four four-square-meter membrane modules in series. The moisture in the raw material and a small amount of ethanol permeate from the downstream side to the downstream side through the membrane module. The upstream side of the membrane is the ethanol product steam with a water content of ≤0.5wt.%, which enters the finished product condenser 25 for condensation after preheating the raw material. The condensed ethanol product is accumulated in the membrane finished product tank 26, and the ethanol product index in the membrane finished product tank 26 is detected. If it is qualified, it is transported to the ethanol product intermediate tank 28 by the membrane finished product pump group 27, and if it is unqualified, it is returned to the ethanol distillate receiving tank 17.

[0075] Step 4: Vacuuming and condensing are adopted on the downstream side of the membrane to form a vapor partial pressure difference between the components on the upstream and downstream sides of the membrane. The permeate vapor enters the permeate condenser unit under the suction of the vacuum unit, and the condensed permeate accumulates in the permeate tank 41. The high and low liquid levels automatically start the permeate pump to transport the permeate to Party A for wastewater treatment. The exhaust port of the vacuum unit is designed with a tail gas condenser 29, and the tail cooling liquid accumulates in the tail gas liquid tank 30. The high and low liquid levels start the tail gas liquid pump 31 to transport it to the raw material buffer tank 1 to recover the ethanol therein.

[0076] The invention objectives of the present utility model embodiment are as follows:

[0077] (1) Add a methanol removal tower and supporting facilities such as a reboiler, condenser, and pump to heat the fusel oil, separate methanol from the top of the tower, and return it to the methanol recovery tower or intermediate tank area of ​​the ethylene glycol distillation system to increase the yield of methanol products.

[0078] (2) Add an ethanol removal tower and supporting facilities such as a reboiler, condenser, and pump. The ethanol and fusel alcohol aqueous solution at the bottom of the methanol removal tower is sent into the tower for heating, and ethanol (ET ≥ 92%) distillate is taken out from the top of the tower.

[0079] (3) Add a molecular sieve membrane dehydration system to dehydrate 92% ethanol, so as to obtain industrial anhydrous ethanol with a purity of ≥ 99.5% with low energy consumption and send it to ethanol storage tanks (for external sale), thereby improving the economic benefits of this project.

[0080] (4) The alcohol-containing wastewater at the bottom of the deethanol tower contains alcohol esters. We consider adding it to the water-coal slurry to replace part of the water and participate in the gasification reaction. Since the wastewater from the fusel oil recovery unit is composed of organic matter and water and does not contain ash, adding the water-coal slurry will not affect the ash melting point of the slurry, so it does not affect the existing operating conditions of the gasifier. The C and H elements contained in it can be fully utilized to produce synthesis gas, realizing the environmentally friendly and clean utilization of organic waste. This move can realize the internal digestion of alcohol-containing wastewater and achieve the goal of pollutant reduction and harmless disposal.

[0081] In summary, compared with the prior art, the embodiments of the present invention have the following beneficial effects:

[0082] 1. The fusel oil raw materials of the technical transformation project of the utility model come from the ethylene glycol distillation system and the methanol distillation system, which are operated at the same time as the main production system. The newly added fusel oil recovery device framework and the existing methanol distillation system are integrated into one, which is regarded as a set of devices, that is, it fully relies on the public engineering of the existing device, and has the advantages of short process, complete supporting facilities and small investment.

[0083] 2. The utility model adopts double-effect distillation heat coupling technology - rationally utilizes the waste heat of the extracted materials to heat the feed, optimizes the heat exchange network, and can effectively reduce the energy consumption of the distillation process. The heat of the feed of the deethanol tower is recycled to improve the energy utilization efficiency and reduce the energy consumption of the system.

[0084] 3. In the fusel oil system of the utility model, ethanol and water will form a minimum azeotrope under normal pressure, which is difficult to separate. Through systematic analysis of the separation effect of the materials in the deethanol tower, high-efficiency tower internals are used to replace the traditional method of using an extractant; at the same time, the purpose of energy saving and consumption reduction and improving economic benefits can be achieved.

[0085] 4. The utility model adopts membrane technology to dehydrate ethanol, which solves the problems of large floor space and inability to handle waste solids in traditional molecular sieve dehydration.

[0086] 5. The utility model utilizes the existing facilities in the factory area to make full use of the alcohol-ester mixture in the wastewater, and uses the wastewater gasification pulping system as pulping water replenishment, which can effectively solve the environmental protection problem.

[0087] It should be noted that, in this article, relational terms such as first and second, etc. are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Moreover, the terms "include", "comprise" or any other variants thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device including a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device. In the absence of further restrictions, the elements defined by the sentence "comprise a ..." do not exclude the presence of other identical elements in the process, method, article or device including the elements.

[0088] The above embodiments are only used to illustrate the technical solutions of the utility model, rather than to limit it; although the utility model is described in detail with reference to the above embodiments, ordinary technicians in this field should understand that they can still modify the technical solutions recorded in the above embodiments, or replace some of the technical features therein by equivalents; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the utility model. .

Claims

1. A device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol, characterized in that: It includes a methanol distillation separation device, an ethylene glycol distillation separation device, a membrane separation device and a permeate treatment device; The outlet of the methanol distillation separation device is connected to the inlet of the ethylene glycol distillation separation device; the outlet of the ethylene glycol distillation separation device is connected to the inlet of the membrane separation device; the outlet of the membrane separation device is connected to the inlet of the permeate treatment device; The methanol distillation separation device comprises a raw material buffer tank (1), a demethanol tower feed pump group (2), a wastewater preheater (3), a condensate preheater (4), a demethanol tower (5), a demethanol tower top condenser (6), a demethanol tower top reflux tank (7), a demethanol tower top reflux pump group (8), a demethanol tower top cooler (9), a methanol recovery intermediate tank (10) and a demethanol tower kettle pump group (11); The raw material buffer tank (1) is connected to the feed port in the middle of the de-methanol tower (5) through the wastewater preheater (3) and the condensate preheater (4) in sequence, and the de-methanol tower feed pump group (2) provides conveying power; A demethanol tower top condenser (6) is provided at the top of the demethanol tower (5); the demethanol tower top condenser (6) is connected to the inlet of the demethanol tower top reflux tank (7); The outlet of the methanol removal tower top reflux tank (7) is connected to the feed inlet at the top of the methanol removal tower (5) and is powered by a methanol removal tower top reflux pump group (8); The outlet of the methanol removal tower top reflux tank (7) is connected to the feed inlet of the methanol recovery intermediate tank (10) through the methanol removal tower top cooler (9), and the transport power is provided by the methanol removal tower top reflux pump group (8); The ethylene glycol rectification and separation device comprises a deethanol tower (12), a deethanol tower top condenser (13), a deethanol tower top reflux tank (14), a deethanol tower top reflux pump group (15), a deethanol tower top cooler (16), an ethanol distillate receiving tank (17), a deethanol tower bottom pump group (18), a wastewater cooler (19) and a coal slurry gasification section device (20); The feed inlet in the middle of the deethanol tower (12) is connected to the kettle of the demethanol tower (5) and is provided with conveying power by the demethanol tower kettle pump group (11); The top of the deethanol tower (12) is provided with a deethanol tower top condenser (13); The deethanol tower top condenser (13) is connected to the inlet of the deethanol tower top reflux tank (14); the outlet of the deethanol tower top reflux tank (14) is connected to the feed inlet of the deethanol tower (12) top and is provided with conveying power by the deethanol tower top reflux pump group (15); The outlet of the deethanol tower top reflux tank (14) is connected to the feed port of the ethanol distillate receiving tank (17) through the deethanol tower top cooler (16) and the conveying power is provided by the deethanol tower top reflux pump group (15); The tower kettle of the deethanol tower (12) is connected to the coal slurry gasification section device (20) through the wastewater preheater (3) and the wastewater cooler (19) in sequence, and the deethanol tower kettle pump group (18) provides transportation power; The membrane separation device comprises a membrane feed pump group (21), a membrane preheater (22), a membrane evaporator (23), a superheater (24), a membrane separation unit, a finished product condenser (25), a membrane finished product tank (26), a membrane finished product pump group (27) and an ethanol finished product intermediate tank (28); The discharge port of the ethanol distillate receiving tank (17) is connected to the inlet of the membrane evaporator (23) through the membrane preheater (22) and the conveying power is provided by the membrane feed pump group (21); The outlet of the film evaporator (23) is connected to the inlet of the membrane separation unit through a superheater (24); The outlet of the membrane separation unit is connected to the inlet of the finished product condenser (25) through the membrane preheater (22); the outlet of the finished product condenser (25) is connected to the inlet of the membrane finished product tank (26); The outlet of the membrane finished product tank (26) is connected to the inlet of the ethanol finished product intermediate tank (28) and the membrane finished product pump group (27) provides the conveying power; The outlet of the membrane finished product tank (26) is connected to the inlet of the ethanol distillate receiving tank (17) and is provided with conveying power by the membrane finished product pump group (27); The outlet of the membrane finished product tank (26) is connected to the inlet of the ethanol finished product intermediate tank (28) and the membrane finished product pump group (27) provides the conveying power; The permeate treatment device comprises a permeate condenser unit, a vacuum unit, a tail gas condenser (29), a tail gas liquid tank (30) and a tail gas liquid pump (31); The permeate condenser unit is connected to the membrane separation unit; The permeate condenser unit is connected to the air inlet of the vacuum unit; the exhaust port of the vacuum unit is provided with a tail gas condenser (29); the tail gas condenser (29) is connected to the feed port of the tail gas liquid tank (30); The discharge port of the tail gas liquid tank (30) is connected to the raw material buffer tank (1) and is provided with conveying power by a tail gas liquid pump (31).

2. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol according to claim 1, characterized in that: The membrane separation unit includes a membrane component one (32), a membrane component two (33), a membrane component three (34), a membrane component four (35), a superheater two (36), a superheater three (37) and a superheater four (38); the inlet of the membrane component one (32) is connected to the superheater one (24), and the superheater two (36) is arranged between the mixed alcohol outlet of the membrane component one (32) and the inlet of the membrane component two (33); the superheater three (37) is arranged between the mixed alcohol outlet of the membrane component two (33) and the inlet of the membrane component three (34); the superheater four (38) is arranged between the mixed alcohol outlet of the membrane component three (34) and the inlet of the membrane component four (35); the mixed alcohol outlet of the membrane component four (35) is connected to the membrane preheater (22).

3. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol according to claim 1, characterized in that: The permeate condenser unit comprises a permeate condenser 1 (39) and a permeate condenser 2 (40); the inlet of the permeate condenser 1 (39) is connected to the permeate outlet of the membrane assembly 1 (32) and the permeate outlet of the membrane assembly 2 (33); the inlet of the permeate condenser 2 (40) is connected to the permeate outlet of the membrane assembly 3 (34) and the permeate outlet of the membrane assembly 4 (35); the outlet of the permeate condenser 1 (39) is connected to the inlet of the permeate condenser 2 (40).

4. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol as claimed in claim 3, characterized in that: The permeate treatment device further comprises a permeate tank (41); the permeate outlet of the first permeate condenser (39) and the permeate outlet of the second permeate condenser (40) are both connected to the feed port of the permeate tank (41).

5. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol as claimed in claim 4, characterized in that: The permeate treatment device further comprises a permeate pump (42) and a wastewater treatment device (43); the discharge port of the permeate tank (41) is connected to the wastewater treatment device (43) and the permeate pump (42) provides conveying power.

6. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol as claimed in claim 3, characterized in that: The vacuum unit comprises a vacuum machine 1 (44) and a vacuum machine 2 (45); the air inlet of the vacuum machine 1 (44) is connected to the outlet of the permeate condenser 2 (40); the exhaust port of the vacuum machine 1 (44) is connected to the air inlet of the vacuum machine 2 (45); the exhaust port of the vacuum machine 2 (45) is connected to the tail gas condenser (29).

7. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol according to claim 1, characterized in that: The methanol distillation separation device further comprises a de-methanol tower reboiler (46); the de-methanol tower reboiler (46) is arranged at the lower part of the de-methanol tower (5).

8. The device for comprehensive utilization of fusel oil byproduct of ethylene glycol co-production of methanol as claimed in claim 7, characterized in that: The de-methanol tower reboiler (46) is configured as a thermal syphon reboiler; the de-methanol tower reboiler (46) uses 0.5 MPaG saturated steam for heating and gasification.

9. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol as claimed in claim 1, characterized in that: The ethylene glycol rectification and separation device further comprises a deethanol tower reboiler (47); the deethanol tower reboiler (47) is arranged at the lower part of the deethanol tower (12).

10. The device for comprehensive utilization of fusel oil by-product of ethylene glycol co-production of methanol according to claim 9, characterized in that: The deethanol tower reboiler (47) is configured as a thermal syphon reboiler; the deethanol tower reboiler (47) uses 0.5 MPaG saturated steam for heating and gasification.

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