CN204385182U - Powder slurry primary heater unit in a kind of Alcohol Production thinning process - Google Patents
Powder slurry primary heater unit in a kind of Alcohol Production thinning process Download PDFInfo
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- CN204385182U CN204385182U CN201520022878.5U CN201520022878U CN204385182U CN 204385182 U CN204385182 U CN 204385182U CN 201520022878 U CN201520022878 U CN 201520022878U CN 204385182 U CN204385182 U CN 204385182U
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Abstract
The utility model discloses powder slurry primary heater unit in a kind of Alcohol Production thinning process, increase pre liquefied tank and a preheating tower, two-stage flash tower is as the thermal source (about-80KPa) of one-level preheating tower, primary flash tower is as the thermal source (about-65KPa) of secondary preheating tower, DDGS exhaust steam is as the thermal source (about-15 to-20KPa) of three grades of preheating towers, control the amount that last step preheating tower enters exhaust steam, after three grades of preheatings, temperature can reach 90-96 DEG C, meets the requirement of technique.The liquefaction temperature of powder slurry is dropped to 90 DEG C by traditional 95 DEG C, has broken people in the understanding of 95 DEG C of liquefaction, the vigor of α-amylase can only be enhanced, promoted liquefaction quality, improve fermented quality.Do not re-use traditional Jet liquefier directly to heat powder slurry, solve 165 DEG C of high-temperature steams and directly contact liquefaction with powder slurry, make α-amylase generating portion inactivation and partial liquefaction mash can be made to produce the impact of caramelize.
Description
Technical field
The utility model relates to Alcohol Production technical field, is specifically related to powder slurry primary heater unit in a kind of Alcohol Production thinning process.
Background technology
Powder mix slurry temperature after our factory saccharification preheating tower can reach about 60 DEG C, Jet liquefier (95 DEG C) through back also needs a large amount of thermals source, existing saccharification two-stage flash tower secondary steam temperature 60 C out, nearly 8 tons per hour, this part heat has all been taken away by the recirculated water in condenser, cause the waste of a large amount of heat energy, also add discharge; DDGS exhaust steam surplus also can be used as thermal source and utilizes.Send into saccharification powder mix slurry temperature-averaging less than 35 DEG C, after one-level preheating, temperature is at about 60 DEG C, does not reach desirable liquefaction temperature, and in pre liquefied tank, liquefaction efficiency is low, affects liquefaction effect.
Alcohol industry liquefaction technology is widely used is that powder slurry steam ejection liquefaction is to the technology of 95 DEG C, more advanced is water heater heating technique in addition, powder slurry is heated to the technique of 95 DEG C after to be high-temperature steam enter the receiving chamber of injector and slip mixing with very high speed by the common ground of this technology, and this kind of heating technique has three shortcomings: consume primary steam; The coking of part sugar can be made, cannot ferment, cause sugared part to lose; The saturation steam that temperatures as high is 165 DEG C directly contacts with powder slurry and makes α-amylase generating portion inactivation.
Powder slurry has the viscosity of about 5 minutes the highest when temperature is 65 degree, if misoperation or occur that what unexpected very easily causes obstruction, so whole operational path must try every possible means to avoid this period in order to avoid equipment blocks, the method for solution has time enough to make the reduction of powder slurry viscosity meet production technique exactly in second pre liquefied tank.In conjunction with physical device situation, we have proposed after powder slurry viscosity reduces by the thinking being pumped into three grades of preheating towers and carrying out preheating.
Utility model content
Problem to be solved in the utility model is to provide powder slurry primary heater unit in a kind of Alcohol Production thinning process, increase pre liquefied tank and a preheating tower, two-stage flash tower is as the thermal source (about-80KPa) of one-level preheating tower, primary flash tower is as the thermal source (about-65KPa) of secondary preheating tower, DDGS exhaust steam is as the thermal source (about-15 to-20 KPa) of three grades of preheating towers, control the amount that last step preheating tower enters exhaust steam, after three grades of preheatings, temperature can reach 90-96 DEG C, meets the requirement of technique.
Powder slurry primary heater unit in a kind of Alcohol Production thinning process, comprise multiple preheating tower, multiple pre liquefied tank, DDGS exhaust steam pipeline, injector, rear liquefied pot, connect pin device and multiple flashing tower, the annexation of this device is: powder mix slurry enters from preheating tower A entrance, described preheating tower A outlet is connected with pre liquefied tank A entrance, described pre liquefied tank A outlet is connected with preheating tower B entrance, described preheating tower B outlet is connected with described pre liquefied tank B entrance, described pre liquefied tank B outlet is connected with described preheating tower C entrance, described preheating tower C outlet is connected with pre liquefied tank C entrance, described pre liquefied tank C outlet is connected with described injector entrance, described injector outlet is connected with described rear liquefied pot entrance, institute's rear liquefied pot of telling outlet is sold device entrance with described company and is connected, the outlet of described even pin device is connected with primary flash tower entrance, described primary flash tower outlet is connected with two-stage flash tower entrance, described two-stage flash tower outlet is connected with brew kettle, the secondary steam outlet of described primary flash tower is connected with described preheating tower B, the secondary steam outlet of described two-stage flash tower is connected with described preheating tower A, described DDGS exhaust steam pipeline is connected with described preheating tower C.
Further, described pre liquefied tank A is connected with described preheating tower B by pump A.
Further, described pre liquefied tank B is connected with described preheating tower C by pump B.
Further, described pre liquefied tank C is connected with described injector by pump C.
Further, described rear liquefied pot is sold device by pump D be connected with described company.
The utility model device powder mix slurry is through new preheating tower A, enter pre liquefied tank A after preheating, be sent to preheating tower B through pump A, after preheating, enter pre liquefied tank B, preheating tower C is sent to through pump B, enter pre liquefied tank C after preheating, be sent to Jet liquefier through pump C, enter rear liquefied pot, be sent to connect through pump D and sell device, enter primary flash tower, then enter two-stage flash tower, finally deliver to brew kettle.The secondary steam outlet of primary flash tower is connected with preheating tower B by steam line, the secondary steam outlet of two-stage flash tower is connected with preheating tower A by steam line, DDGS exhaust steam pipeline is connected with preheating tower C, the secondary steam of primary flash tower is as the thermal source of preheating tower B, the secondary steam of two-stage flash tower is as the thermal source of preheating tower A, DDGS exhaust steam is as the thermal source of preheating tower C, after one-level preheating changes three grades of preheatings into, heat makes full use of, reach and do not re-use primary steam, the less discharge of sewage.
DDGS exhaust steam water of condensation is on the demonstration of thinning, fermenting process impact: simulate large production technique, thinning is carried out to the process water and 0.025% exhaust steam water of condensation that add 0.025% in raw material powder slurry respectively, record DE value and the conversion coefficient of post liquefaction powder slurry, though the DE value after powder is slurried and the rare reduction before and after use DDS exhaust steam of the conversion coefficient after saccharification, within the fluctuation range of normal production data.Large impact can not be caused to production.According to the consumption of preheating powder slurry exhaust steam, we simulate large each processing condition of producing and have made the impact of cultivating distiller's yeast after DDS exhaust steam adds large production powder slurry, on the impact of fermentation results, in cultivating at distiller's yeast, saccharomycetic bacterial strain advantage is comparatively strong, it is vigorous to grow, its impact on yeast normal growth may be covered, therefore, also will test fermenting process.The data that each sample fermenting process and fermentation end can be found out, the time that each experiment reaches fermentation termination is also more or less the same, the acidity of experimental result and all more satisfactory containing capacity for liquor, fermentation end of a period index in actual production more should be better than the result tested, and each sample all can reach the requirement of Alcohol Production.
The beneficial effect of this new technique:
1) liquefaction temperature of powder slurry is dropped to 90 DEG C by traditional 95 DEG C, broken people in the understanding of 95 DEG C of liquefaction, the vigor of α-amylase can only be enhanced, promoted liquefaction quality, improve fermented quality.
2) do not re-use traditional Jet liquefier directly to heat powder slurry, solve 165 DEG C of high-temperature steams and directly contact liquefaction with powder slurry, make α-amylase generating portion inactivation and partial liquefaction mash can be made to produce the impact of caramelize.Adopt the new technology of three grades of preheatings, change traditional technique thinking completely, in the same industry, there is top standard.After this technology implementation, become history by the technique that Jet liquefier heats up, this novel process reach of the same trade in advanced level, and after actual verification uses in production, improve that powder is slurried, distiller's yeast, fermented quality, achieve remarkable effect.
3) adopt the method for vacuum extraction that the exhaust steam of low pressure is entered in powder slurry preheating tower, make exhaust steam and powder slurry carry out thermal exchange in preheating tower, solve the use of low pressure exhaust steam, transportation problem.Utilize exhaust steam to heat powder slurry, solve the unserviceable difficult problem of low-temperature steam exhaust that DDGS drying produces, eliminate environmental pollution, reduce the energy consumption of alcohol production, the pH value of powder slurry declines 0.3, and the effective miscellaneous bacteria that suppresses is bred, and improves liquefaction mash, distiller's yeast, fermented quality.
4) this technology is the autonomous innovation of Henan alcohol fuel factory of Tian Guan alcohol fuel company limited, compare with employing Jet liquefier technique in ethanol industry after using, liquefy and per hourly save primary steam 12 tons, saccharification workshop section substantially no longer uses primary steam, the ton alcohol steam consumption can decline about 0.4 ton, year reduces production cost about 1,100 ten thousand yuan, is worth in industry applying.
5) secondary steam of flashing tower is utilized, do not need the energy that provides specially to heat preheating tower A and preheating tower B, save the energy further and decrease the discharge of sewage.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the utility model is further described:
Fig. 1 is the structural representation of powder slurry primary heater unit in the utility model Alcohol Production thinning process.
Embodiment
As shown in Figure 1: the utility model provides powder slurry primary heater unit in a kind of Alcohol Production thinning process, comprise multiple preheating tower, multiple pre liquefied tank, DDGS exhaust steam pipeline, injector, rear liquefied pot, connect pin device and multiple flashing tower, the annexation of this device is: powder mix slurry enters from preheating tower A entrance, described preheating tower A outlet is connected with pre liquefied tank A entrance, described pre liquefied tank A outlet is connected with preheating tower B entrance, described preheating tower B outlet is connected with described pre liquefied tank B entrance, described pre liquefied tank B outlet is connected with described preheating tower C entrance, described preheating tower C outlet is connected with pre liquefied tank C entrance, described pre liquefied tank C outlet is connected with described injector entrance, described injector outlet is connected with described rear liquefied pot entrance, institute's rear liquefied pot of telling outlet is sold device entrance with described company and is connected, the outlet of described even pin device is connected with primary flash tower entrance, described primary flash tower outlet is connected with two-stage flash tower entrance, described two-stage flash tower outlet is connected with brew kettle, the secondary steam outlet of described primary flash tower is connected with described preheating tower B, the secondary steam outlet of described two-stage flash tower is connected with described preheating tower A, described DDGS exhaust steam pipeline is connected with described preheating tower C.Described pre liquefied tank A is connected with described preheating tower B by pump A.Described pre liquefied tank B is connected with described preheating tower C by pump B.Described pre liquefied tank C is connected with described injector by pump C.Described rear liquefied pot is sold device by pump D with described company and is connected.
Powder mix slurry is through new preheating tower A, enter pre liquefied tank A after preheating, be sent to preheating tower B through pump A, after preheating, enter pre liquefied tank B, preheating tower C is sent to through pump B, enter pre liquefied tank C after preheating, be sent to Jet liquefier through pump C, enter rear liquefied pot, be sent to connect through pump D and sell device, enter primary flash tower, then enter two-stage flash tower, finally deliver to brew kettle.The secondary steam outlet of primary flash tower is connected with preheating tower B, the secondary steam outlet of two-stage flash tower is connected with preheating tower A, DDGS exhaust steam pipeline is connected with preheating tower C, DDGS exhaust steam is as the thermal source of preheating tower C, the method of vacuum extraction is adopted to make the exhaust steam of low pressure enter in powder slurry preheating tower, exhaust steam and powder slurry is made to carry out thermal exchange in preheating tower, solve the use of low pressure exhaust steam, transportation problem, the secondary steam of primary flash tower is as the thermal source of preheating tower B, the secondary steam of two-stage flash tower is as the thermal source of preheating tower A, after one-level preheating changes three grades of preheatings into, heat makes full use of, reach and do not re-use primary steam, the less discharge of sewage.
Claims (5)
1. powder slurry primary heater unit in an Alcohol Production thinning process, it is characterized in that: comprise multiple preheating tower, multiple pre liquefied tank, DDGS exhaust steam pipeline, injector, rear liquefied pot, connect pin device and multiple flashing tower, the annexation of this device is: powder mix slurry enters from preheating tower A entrance, described preheating tower A outlet is connected with pre liquefied tank A entrance, described pre liquefied tank A outlet is connected with preheating tower B entrance, described preheating tower B outlet is connected with described pre liquefied tank B entrance, described pre liquefied tank B outlet is connected with described preheating tower C entrance, described preheating tower C outlet is connected with pre liquefied tank C entrance, described pre liquefied tank C outlet is connected with described injector entrance, described injector outlet is connected with described rear liquefied pot entrance, institute's rear liquefied pot of telling outlet is sold device entrance with described company and is connected, the outlet of described even pin device is connected with primary flash tower entrance, described primary flash tower outlet is connected with two-stage flash tower entrance, described two-stage flash tower outlet is connected with brew kettle, the secondary steam outlet of described primary flash tower is connected with described preheating tower B, the secondary steam outlet of described two-stage flash tower is connected with described preheating tower A, described DDGS exhaust steam pipeline is connected with described preheating tower C.
2. powder slurry primary heater unit in Alcohol Production thinning process as claimed in claim 1, is characterized in that: described pre liquefied tank A is connected with described preheating tower B by pump A.
3. powder slurry primary heater unit in Alcohol Production thinning process as claimed in claim 1, is characterized in that: described pre liquefied tank B is connected with described preheating tower C by pump B.
4. powder slurry primary heater unit in Alcohol Production thinning process as claimed in claim 1, is characterized in that: described pre liquefied tank C is connected with described injector by pump C.
5. powder slurry primary heater unit in Alcohol Production thinning process as claimed in claim 1, is characterized in that: described rear liquefied pot is sold device by pump D with described company and is connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520022878.5U CN204385182U (en) | 2015-01-14 | 2015-01-14 | Powder slurry primary heater unit in a kind of Alcohol Production thinning process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520022878.5U CN204385182U (en) | 2015-01-14 | 2015-01-14 | Powder slurry primary heater unit in a kind of Alcohol Production thinning process |
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| CN204385182U true CN204385182U (en) | 2015-06-10 |
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| CN201520022878.5U Expired - Fee Related CN204385182U (en) | 2015-01-14 | 2015-01-14 | Powder slurry primary heater unit in a kind of Alcohol Production thinning process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107287261A (en) * | 2016-03-30 | 2017-10-24 | 郑州大学 | A kind of liquefying starchiness raw material saccharification waste heat reclaiming process |
| CN110511864A (en) * | 2019-08-28 | 2019-11-29 | 宿州市皖神面制品有限公司 | A kind of thinning workshop section multiple-effect tandem flash distillation energy saving technique |
-
2015
- 2015-01-14 CN CN201520022878.5U patent/CN204385182U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107287261A (en) * | 2016-03-30 | 2017-10-24 | 郑州大学 | A kind of liquefying starchiness raw material saccharification waste heat reclaiming process |
| CN110511864A (en) * | 2019-08-28 | 2019-11-29 | 宿州市皖神面制品有限公司 | A kind of thinning workshop section multiple-effect tandem flash distillation energy saving technique |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150610 Termination date: 20170114 |