CN210438723U - Wide-channel plate type mash heat exchanger for producing alcohol by cassava - Google Patents
Wide-channel plate type mash heat exchanger for producing alcohol by cassava Download PDFInfo
- Publication number
- CN210438723U CN210438723U CN201921074442.5U CN201921074442U CN210438723U CN 210438723 U CN210438723 U CN 210438723U CN 201921074442 U CN201921074442 U CN 201921074442U CN 210438723 U CN210438723 U CN 210438723U
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- mash
- exchange medium
- heat exchanger
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Alcoholic Beverages (AREA)
Abstract
The utility model provides a wide-channel plate-type mash heat exchanger for producing alcohol by cassava, which comprises a mash heat exchanger shell, a heat exchange medium circulation channel, a heat exchange core, a heat exchange mash inlet, a heat exchange mash outlet, a heat exchange medium inlet and a heat exchange medium outlet, wherein the heat exchange medium inlet, the heat exchange medium outlet, the heat exchange mash inlet and the heat exchange mash outlet are positioned on the mash heat exchanger shell and are respectively communicated with the heat exchange medium circulation channel and the heat exchange medium circulation channel of the heat exchange core; heat exchange mediumEach plate of the flow passage is fixedly connected with the other plate by a point-type distance column and is changed into a square steel bar for fixed welding. The utility model discloses through each board of heat exchange medium circulation passageway and the fixed welding of square steel bar that changes into by point type distance post fixed connection between the board and solved the transport problem of high concentration mash, its mash concentration can reach 25Bx。The above.
Description
Technical Field
The utility model belongs to the technical field of indirect heating equipment, in particular to wide-passage plate-type mash heat exchanger.
Background
In the process of producing edible alcohol by using starchy raw materials, a liquid saccharification working section is a very critical working procedure, and the energy consumption and the starch utilization rate of production are directly influenced. The existing process has two types: one is the vacuum cooling of the liquefied mash, and the other is the one-step cooling of the spiral plate heat exchanger. The disadvantages of the vacuum cooling and cooling method are: the material temperature control cannot be well adjusted in the range required by the process, namely the material temperature control is unstable; the cooling method of the spiral plate heat exchanger has the following defects: under the condition of high concentration, the mash has high viscosity and is difficult to convey, and meanwhile, the heat exchanger is easy to block, the cooling effect is poor, and the heat loss is large.
The invention discloses a wide-channel plate heat exchanger with the Chinese patent application publication number of CN105841525A, and the invention name is a wide-channel plate heat exchanger, which comprises a support, a shell, a heat exchange core body, a heat exchange medium inlet, a heat exchange medium outlet, a heat exchange medium inlet and a heat exchange medium outlet, wherein the heat exchange medium inlet, the heat exchange medium outlet, the heat exchange medium inlet and the heat exchange medium outlet are positioned on the shell and are communicated with the heat exchange core body, the heat exchange core body comprises a heat exchange medium circulation channel and a heat exchange medium circulation channel, the heat exchange medium circulation channel is provided with a plurality of nest-shaped turbulent chambers, and the shell. In order to avoid the heat exchange medium cutoff caused by the elastic deformation of the heat exchange plate when the pressure of the heat exchange medium is larger, the arc-shaped supporting pieces are arranged at the necks of the heat exchange medium flowing channel in pairs in the embodiment, so that the expansion of the heat exchange medium flowing channel is not influenced, the minimum size of the cross section of the heat exchange medium flowing channel is ensured, and the normal flowing of the heat exchange medium is further ensured.
Support columns are welded between the two sheets of the wide-channel plate type mash heat exchanger and form plate pairs, and the adjacent two plate pairs form a process channel; (see figure 6) and point distance columns are arranged in the channel, and the concentration of the cassava mash can reach 25Bx。The cassava mash is easy to be blocked by impurities on the dot-shaped distance column and cleanedThe time frequency is high, and the production efficiency is seriously influenced. How to combine and solve the technical problems that the mash of the heat exchange medium has low flow velocity in a flow channel, poor cooling effect and large heat loss and is required to be solved in the process of producing edible alcohol.
Disclosure of Invention
The invention aims to solve the technical problem of providing a wide-channel plate heat exchanger with low channel flow speed, poor cooling effect and large heat loss.
The technical scheme of the utility model is realized like this:
a wide-channel plate-type mash heat exchanger for producing alcohol from cassava comprises a mash heat exchanger shell, a heat exchange medium circulation channel, a heat exchange core body, a heat exchange mash inlet, a heat exchange mash outlet, a heat exchange medium inlet and a heat exchange medium outlet, wherein the heat exchange medium inlet, the heat exchange medium outlet, the heat exchange mash inlet and the heat exchange mash outlet are positioned on the mash heat exchanger shell and are respectively communicated with the heat exchange medium circulation channel and the heat exchange medium circulation channel of the heat exchange core body;
the plates of the heat exchange medium flow channel are fixedly connected by point-type distance columns and are changed into square steel bars for fixed welding.
Furthermore, the section of the square steel bar is 12 x 12mm, and the length of the square steel bar is matched with the length of the heat exchange medium flowing channel.
Further, the height of the plate type mash heat exchanger channel is 12mm, and the width of the plate type mash heat exchanger channel is 100 mm.
The utility model discloses through each board of heat exchange medium circulation passageway and the fixed welding of square steel bar that changes into by point type distance post fixed connection between the board and solved the transport problem of high concentration mash, its mash concentration can reach 25Bx。The above.
The height of the plate-type mash heat exchanger channel of 12mm and the width of 100mm are the best data for the delivery of high-concentration mash.
Drawings
Fig. 1 and fig. 2 are schematic structural views of a system for producing edible alcohol by using cassava according to the present invention;
FIG. 3 is a schematic structural view of the mash heat exchanger of the present invention;
FIG. 4 is a schematic illustration of spot-to-spot column distribution for mash heat exchangers of the prior art;
FIG. 5 is a schematic view of a square steel bar structure of a mash heat exchanger;
FIG. 6 is a perspective view of a spot-type distance column of the mash heat exchanger of the prior art;
1-sand removal front tank; 2-a sand removal pump; 3-a desander; 4-stirring tank; 5-a material mixing pump; 6-1# front liquefaction tank; 7-1# mash heat exchange pump; 8-1# mash heat exchanger; 9-2# front liquefaction tank; 10-3# front liquefaction tank; 11-a cooking feed pump; 12-a hydrojet liquefier; 13-an after-ripening device; 14-a digester pump; 15-primary water self-pipe network; 16-1# post liquefaction tank; outlet of 161-1# mash heat exchanger; 17-2# post liquefaction tank; 18-post liquefaction pump; 19-2# mash heat exchanger; 20-concentrated sulfuric acid tank; 21-1# saccharification tank; 22-saccharifying enzyme tank; 23-2# saccharification tank; 24-saccharification discharge pump.
81-mash heat exchanger shell; 82-heat exchange medium flow channels; 83-heat exchange medium flow channels; 84-a heat exchange core; 85-heat exchange medium inlet; 86 heat exchange medium outlet; 87-heat exchange medium inlet; 88-point distance-fixing pole; 89-heat exchange medium outlet; 84-1-heat exchange plate; 88-1-square steel strip.
Detailed Description
The following detailed description of the embodiments of the present invention is provided with reference to the accompanying drawings:
mash: the mixture of the materials and water in the edible alcohol production by the fermentation method.
The production of edible alcohol by using cassava as a raw material is as an example:
the process flow is briefly described as follows:
1. the method comprises the steps of crushing raw materials cassava, adding process water through stirring, feeding the crushed raw materials into a desanding front tank, uniformly stirring to obtain cassava powder slurry, pumping the cassava powder slurry into a desander through a desanding pump to remove silt mixed in the raw materials, and feeding the cassava powder slurry into a material mixing tank.
2. Adding high-temperature resistant α amylase (hereinafter referred to as liquefying enzyme) into the material mixing tank according to 6 units/gram of raw material, stirring uniformly, pumping to a No. 2 mash heat exchanger through a material mixing pump, exchanging heat with liquefied mash in a No. 2 rear liquefying tank, heating to 55-60 ℃, simultaneously cooling the liquefied mash to 55-60 ℃ from 75-80 ℃, and feeding the 55-60 ℃ slurry after heat exchange into a No. 1 front liquefying tank.
3. The temperature of the front liquefaction tank No. 1 is increased to 65-70 ℃ by steam, the gelatinization temperature of cassava is reached, the liquefaction enzyme starts to act, the viscosity of slurry is obviously reduced, and the transportation is not difficult.
4. The material is pumped from the front 1# liquefaction tank to the 1# mash heat exchanger through the 1# mash circulation heat pump to exchange heat with the cooked mash coming out of the after-ripening device, the temperature is raised to 80-85 ℃, the cooked mash enters the front 2# liquefaction tank, meanwhile, the temperature of the cooked mash is reduced to 75-80 ℃ from 90-95 ℃, and the cooked mash enters the rear 1# liquefaction tank.
5. The temperature of the liquefaction tanks before No. 2 and No. 3 is controlled to be 80-85 ℃, and the temperature is the optimal action temperature of the liquefaction enzyme.
6. The material is uniformly mixed and heated with steam by a steam feed pump through a jet liquefier and then enters an after-ripening device, and the temperature of the after-ripening device is controlled at 90-95 ℃.
7. The material is cooled by a 1# mash heat exchanger after coming out of the after-ripening device and then enters a 1# post-liquefaction tank, and meanwhile, the 1# post-liquefaction tank is added with liquefaction enzyme according to 4 units/gram of raw material.
8. Pumping the material from the No. 2 post-liquefaction tank to the No. 2 mash heat exchanger through a post-liquefaction pump, cooling to 55-60 ℃, feeding the material into a saccharification tank, and adding saccharifying enzyme into the saccharification tank.
Secondly, various process control indexes are as follows:
1. and (3) crushing particle size: ∅ 1.6.6-1.8 m material mixing temperature: 35-40 DEG C
Mixing and adding water: 1: 2.3-2.5 of the mixing concentration: 25-26 BX degree
2. Adding amount of liquefying enzyme in the front liquefying tank of No. 1: 6 units/gram of raw material
Pre-1 liquefaction tank temperature: 65-70 deg.C
1# pre-liquefaction tank residence time: 30-40 min
2# and 3# front liquefaction tank temperature: 80-85 DEG C
2# and 3# front liquefaction tank residence time: 60-90 min
3. Jet liquefier temperature: 90-95 DEG C
After-ripening vessel residence time: 40-60 min
4. Adding amount of liquefying enzyme in post-liquefaction tank No. 1: 4 units/gram of raw material
Temperature of the post-liquefaction tank: 75-80 DEG C
Residence time of the post-liquefaction tank: 60-90 min
5. Adding amount of saccharifying enzyme in saccharifying tank: 150 to 200 units/g of raw material,
Temperature of the saccharification tank: 55-60 DEG C
Residence time of saccharification tank: 40-60 min.
Referring to fig. 3, the mash heat exchanger comprises a mash heat exchanger housing 81, a heat exchange medium flow channel 82, a heat exchange medium flow channel 83, a heat exchange core 84, a heat exchange mash inlet 85, a heat exchange mash outlet 89, a heat exchange medium inlet 87, and a heat exchange medium outlet 66, wherein the heat exchange medium inlet 85, the heat exchange medium outlet 89, the heat exchange mash inlet 13, and the heat exchange mash outlet 87 are located on the mash heat exchanger housing and are communicated with the heat exchange core 84.
The mash heat exchanger shell 81 is of a combined structure and is formed by connecting 4 side plates from top to bottom and from front to back through bolts, and end covers are arranged at two ends of the mash heat exchanger shell 81, so that the mash heat exchanger shell 81 can be completely disassembled, and the installation and the maintenance are very convenient.
The heat exchange medium inlet 85, the heat exchange medium outlet 89, the heat exchange mash inlet 87 and the heat exchange mash outlet 86 are respectively positioned at the two ends of the front and the rear side plates.
Compared with the cassava mash heat exchanger, the layer number and the width of the heat exchange plates 84-1 are much larger than those of other common mash heat exchangers, the heat exchange medium among the heat exchange plates 84-1 is cut off due to elastic deformation of the heat exchange plates 84-1 when the pressure of the heat exchange medium is higher in the prior art, the plates and the plates (plates) are fixedly connected by virtue of a point-type distance column, and when the cassava mash passes through, because the cassava mash has high concentration and contains a large amount of fibers, blockage is easily formed on the distance column (equivalent to the supporting piece 25 in the background art) when the cassava mash is directly used.
In this embodiment, the fixing of the plates in the heat exchange medium flow passage 82 is changed from fixing by point-type distance columns to fixing by square steel bars 88-1, i.e., the heat exchange core 84 is composed of a plurality of heat exchange plates 84-1 and two side partition plates which adopt the direction bars 88-1 along the mash forward direction.
By the above modification, the heat exchange medium flow passage 82, which originally flows in a sheet-like manner, is changed into individual passages.
In the prior art, because the point-type distance pillars 88 are point-type, impurities in cassava mash can be hung on the point-type distance pillars 88 and can be blocked quickly, the cleaning time frequency is high, and the production efficiency is seriously influenced.
After the point type of the distance column is changed into the square steel bar 88-1, the cassava mash has no hanging point and smoothly passes through the channel.
In order to further overcome the easy blockage of the mash heat exchanger, the height of the plate heat exchanger channel is 12mm, and the width of the plate heat exchanger channel is changed into 100 mm.
This does not affect the expansion of the heat exchange medium flow channel 82 and at the same time ensures that the cassava mash of the cross section of the heat exchange medium flow channel 82 is of a relatively optimal size, thereby ensuring the normal flow of the heat exchange medium.
The mash heat exchanger of the utility model is not improved, and is maintained almost for two and three weeks, and can normally work only by maintaining in three months after improvement.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention should be covered by the present invention.
Claims (3)
1. A wide-channel plate-type mash heat exchanger for producing alcohol from cassava comprises a mash heat exchanger shell, a heat exchange medium circulation channel, a heat exchange core body, a heat exchange medium inlet, a heat exchange medium outlet, a heat exchange medium inlet and a heat exchange medium outlet, wherein the heat exchange medium inlet, the heat exchange medium outlet, the heat exchange mash inlet and the heat exchange mash outlet are positioned on the mash heat exchanger shell and are respectively communicated with the heat exchange medium circulation channel and the heat exchange medium circulation channel of the heat exchange core body;
the heat exchange medium circulation channel is characterized in that each plate of the heat exchange medium circulation channel is fixedly connected with a square steel bar through a point-type distance column, and the square steel bar is fixedly welded.
2. The wide channel plate mash heat exchanger according to claim 1, characterized in that the square steel bars have a cross-section of 12 x 12mm and a length adapted to the length of the heat exchange medium flow channels.
3. The wide channel plate mash heat exchanger according to claim 1, characterised in that the height of the plate mash heat exchanger channels is 12mm and the width is 100 mm.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821081565 | 2018-07-10 | ||
| CN2018210815657 | 2018-07-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210438723U true CN210438723U (en) | 2020-05-01 |
Family
ID=70405101
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921074442.5U Active CN210438723U (en) | 2018-07-10 | 2019-07-10 | Wide-channel plate type mash heat exchanger for producing alcohol by cassava |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210438723U (en) |
-
2019
- 2019-07-10 CN CN201921074442.5U patent/CN210438723U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN2873744Y (en) | Device for quick preparing industrial ammonia water | |
| CN210438723U (en) | Wide-channel plate type mash heat exchanger for producing alcohol by cassava | |
| CN102776075B (en) | Interactive turbulent flow reaction device | |
| CN202039062U (en) | Combine device for producing cellulosic ethanol through fermenting xylose and simultaneously separating ethanol | |
| CN210438709U (en) | A saccharification system for cassava production alcohol | |
| CN101839655B (en) | High-efficiency module back-stroke displacement heat exchanger | |
| CN210826189U (en) | Starch liquefaction saccharification pilot plant | |
| CN110551513A (en) | Multi-pipe-layer asphalt falling film cooler and asphalt cooling forming process applying same | |
| CN204996456U (en) | Horizontal alkylation reaction ware of vibration proof | |
| CN210438712U (en) | Cooling device for making wine | |
| CN209873049U (en) | Zinc pressure leaching device | |
| CN207468644U (en) | A kind of production equipment of alcohol fuel | |
| CN209019933U (en) | A kind of rectifier unit | |
| CN203108234U (en) | Hybrid evaporimeter | |
| CN209810134U (en) | Sectional temperature control reaction device | |
| CN216890854U (en) | Supercritical energy-saving production system suitable for biodiesel | |
| CN104248939A (en) | Methanol oxidizer in silver catalyst process formaldehyde device | |
| CN220250781U (en) | Monosodium glutamate crystallization tail gas cooling system | |
| CN2835227Y (en) | Low-pressure treatment device for waste liquid from synthetic ammonia and urea | |
| CN216205550U (en) | Mash heat exchanger, fuel ethanol liquefied mash treatment system and waste mash treatment system | |
| CN217856019U (en) | High-efficient pressurization evaporation crystallization device of battery level sulphuric acid | |
| CN221309563U (en) | Flash evaporation isomerism system | |
| CN213866265U (en) | Glucose cooling and saccharifying device | |
| CN211963118U (en) | Energy-saving distillation device for preparing fuel ethanol | |
| CN207299104U (en) | A kind of high efficiency energy saving heat exchanging unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |