CN204509362U - A kind of balance of the automatic steam for sugar refining technology heat riser - Google Patents
A kind of balance of the automatic steam for sugar refining technology heat riser Download PDFInfo
- Publication number
- CN204509362U CN204509362U CN201520003552.8U CN201520003552U CN204509362U CN 204509362 U CN204509362 U CN 204509362U CN 201520003552 U CN201520003552 U CN 201520003552U CN 204509362 U CN204509362 U CN 204509362U
- Authority
- CN
- China
- Prior art keywords
- steam
- pipeline
- juice
- control valve
- flow control
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/14—Combined heat and power generation [CHP]
Landscapes
- Control Of Turbines (AREA)
Abstract
A kind of balance of the automatic steam for sugar refining technology heat riser of the present utility model belongs to sugar refining technology technical field.This automatic steam balance heat riser comprises: heat exchanging apparatus, and this heat exchanging apparatus is located on III effect juice steam pipeline, and is connected with steam turbine waste vapour pipeline with the second connecting tube by the first connecting tube; Steam flow control valve, this steam flow control valve is located at steam and is flowed into and flow out on the pipeline of heat exchanging apparatus; PLC, this PLC control the operation of steam flow control valve.It is simple and efficiency utilization existing resource can realize the features such as energy-conservation that the technical solution of the utility model has structure.
Description
Technical field
The utility model relates to sugar refining technology technical field, particularly relates to a kind of automatic steam for sugar refining technology balance heat riser.
Background technology
The live steam amount that sugar refining technology vapour directly supplements from the displacement after turbine driven set generating and boiler, belong to cogeneration operation scheme, inadequate Closed Circulation in Sugar Production (the pressure 0.294MPa of turbine driven set displacement due to most sugar refinery, temperature 180 DEG C or pressure 0.49MPa, temperature 230 DEG C), also must directly supply superheated vapour (pressure 3.82MPa from boiler, temperature 450 DEG C or pressure 2.45MPa, the superheated vapour of temperature 390 DEG C of two kinds of parameters) again through spray atomizing, desuperheat step-down becomes the lower saturation steam of quality (pressure about 0.2MPa, temperature about 130 DEG C) use, there is intrinsic Irreversible factor operational mode in this Closed Circulation in Sugar Production, the theoretical thermal equilibrium of cogeneration is not reached in actual production, all there is 5t/h in the sugar enterprise of general daily squeezed quantity more than 2000 tons---the even more Boiler Steam magnitude of recruitment of 30t/h, the calorific loss that the live steam that boiler supplements causes more is larger, consume energy also higher.
Many sugar enterprise technician adopt various diverse ways to extract evaporation III, IV effect juice steam in discussion to be back to and to boil sugar as far as possible all the time, make sugar refining technology vapour can use juice vapour comprehensively, reduce thermosteresis, comprise and think that raising I is imitated into methods such as pressure tank and temperature, plate-type heat exchanger, flue gas heating, but acquired effect not very desirable.Existing sugar refining technology vapo(u)rization system extraction juice vapour enters boiling pan and heats, and generally only use evaporation I, II and imitate tank juice vapour, small part sugar refinery can be used III effect juice steam and be boiled sugar, and also Yin Wendu is low, poor effect.And III, IV effect tank juice vapour reuse is extracted because its temperature is low with micro-vacuum in most sugar refinery, cannot reuse to need temperature higher than more than 98 DEG C and need certain pressure use vapour unit, as: juice I and II heats and vapour department used by triose etc. clearly.From the V last tank of effect juice vapour amount out (steam of about 4%-7% and sugarcane ratio), discharge after these juice vapour all adopt injection condensing, cause larger heat economy loss.The current evaporation III, IV in most sugar refinery is imitated tank juice vapour and substantially can be used in mixing juice heating, and small part sugar enterprise can be used in III effect juice steam and boil methose vapour.
Utility model content
In order to solve the problems of the technologies described above, the purpose of this utility model is to provide a kind of automatic steam for sugar refining technology balance heat riser, and this automatic steam balance heat riser can effectively heat boiling pan, has carried out efficient utilization to existing resource.
The purpose of this utility model is achieved through the following technical solutions:
A kind of balance of the automatic steam for sugar refining technology heat riser, comprise heat exchanging apparatus, described heat exchanging apparatus is tube bundle heat exchanger, and described tube bundle heat exchanger is located on III effect juice steam pipeline, and is connected with steam turbine waste vapour pipeline with the second connecting tube by the first connecting tube; Described heat exchanging apparatus is provided with high-pressure side steam inlet, high-pressure side vapour outlet, low pressure end juice vapor inlet and low pressure end juice vapour outlet, wherein, the front-end pipelines that described high-pressure side steam inlet flows into by the first connecting tube and steam turbine waste vapour bucket of lowering the temperature is connected, and the first connecting tube is provided with the first steam flow control valve, the rear end pipeline that described high-pressure side vapour outlet flows out by the second connecting tube and steam turbine waste vapour bucket of lowering the temperature is connected; Described low pressure end juice vapor inlet and low pressure end juice vapour outlet are located on same axis, and the 3rd pipeline be connected with low pressure end juice vapour outlet is provided with the second steam flow control valve; Steam flow control valve, described steam flow control valve is located at steam and is flowed into and flow out on the pipeline of heat exchanging apparatus; PLC, described PLC controls the operation of steam flow control valve.
For an automatic steam balance heat riser for sugar refining technology, it comprises:
Heat exchanging apparatus, described heat exchanging apparatus is located on III effect juice steam pipeline, and is connected with steam turbine waste vapour pipeline with the second connecting tube by the first connecting tube;
Steam flow control valve, described steam flow control valve is located at steam and is flowed into and flow out on the pipeline of heat exchanging apparatus;
PLC, described PLC controls the operation of steam flow control valve.
By above-mentioned the technical solution of the utility model, automatic steam for sugar refining technology balance heat riser of the present utility model by adding heat exchanging apparatus on existing III effect juice steam pipeline, and heat exchanging apparatus is connected with steam turbine waste vapour pipeline, steam turbine waste vapour is made directly to add effect juice steam and heat boiling pan, and then substantially increase the utilization ratio of resource, be conducive to energy-conserving and environment-protective.
Accompanying drawing explanation
Fig. 1 is a kind of embodiment structural representation of automatic steam of the present utility model balance heat riser;
Fig. 2 is a kind of embodiment structural representation of heat exchanging apparatus of the present utility model.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in detail:
As depicted in figs. 1 and 2, a kind of balance of the automatic steam for sugar refining technology heat riser, it comprises heat exchanging apparatus 100, first steam flow control valve 91 and PLC (programmable logic controller) 90, wherein:
Heat exchanging apparatus 100 is tube bundle heat exchanger, described heat exchanging apparatus 100 is located on III effect juice steam pipeline, and then III effect juice steam pipeline is divided into the 3rd pipeline 11 near boiling pan 32 and the 4th pipeline 12 near evaporating pot 42,3rd pipeline 11 is connected by inlet mouth 21 with the heating steam drum 31 being located at boiling pan 32 bottom, and heating steam drum 32 is also provided with the 5th pipeline 16 that outer steam discharge coagulates water.The bottom of evaporating pot 42 is provided with steam drum 41, and steam drum 41 is provided with the 6th pipeline 17 and the 7th pipeline the 18, six pipeline 17 inputs to steam drum 41 for evaporating juice vapour from upper level, and the 7th pipeline 18 is for arranging air condensate outward.The 8th pipeline 19 going to next stage evaporating pot is provided with on evaporating pot 42 top.Meanwhile, heat exchanging apparatus 100 is connected with steam turbine waste vapour pipeline 13 with the second connecting tube 15 by the first connecting tube 14.
First steam flow control valve 91, the first described steam flow control valve 91 is located at steam and is flowed into and flow out on the pipeline (the first connecting tube 14, second connecting tube 15) of heat exchanging apparatus.First steam flow control valve 91 is for controlling the steam flow flowing into and flow out heat exchanging apparatus 100.
PLC90, described PLC90 controls the operation of steam flow control valve.
As shown in Fig. 2 and Fig. 1, described heat exchanging apparatus 100 is provided with high-pressure side steam inlet 10 (as shown in Figure 1, high-pressure side steam inlet 10 is connected with the first port 22 of the first connecting tube 14), high-pressure side vapour outlet 30 (as shown in Figure 1, high-pressure side vapour outlet 30 is connected with the port 23 of the second connecting tube 15, another second port 24 of second connecting tube 15 is connected with steam turbine waste vapour pipeline 13), low pressure end juice vapor inlet 20 (as shown in Figure 1, low pressure end juice vapor inlet 20 is connected with the port of the 4th pipeline 12, another port of 4th pipeline 12 is connected with evaporating pot 42) and low pressure end juice vapour outlet 40 is (as shown in Figure 1, low pressure end juice vapour outlet 40 is connected with the port of the 3rd pipeline 11, another port of 3rd pipeline 11 is connected with heating steam drum 31), wherein, the front-end pipelines that described high-pressure side steam inlet 10 flows into by the first connecting tube 14 and steam turbine waste vapour bucket 51 (i.e. pipeline cooler) of lowering the temperature is connected, and the first connecting tube 14 is provided with the first steam flow control valve 91 (namely the first steam flow control valve 91) as shown in Figure 2, the rear end pipeline that described high-pressure side vapour outlet 30 flows out by the second connecting tube 15 and steam turbine waste vapour bucket 51 of lowering the temperature is connected.Described low pressure end juice vapor inlet 20 and low pressure end juice vapour outlet 40 are located on same axis, and the 3rd pipeline 11 be connected with low pressure end juice vapour outlet 40 is provided with the second steam flow control valve 92.First steam flow control valve 91 and the second steam flow control valve 92 are by PLC90 red-tape operati.
Meanwhile, described heat exchanging apparatus 100 is also provided with multiple sewage draining exit (50,60,70 and 80), so that waste water is discharged.
The technical solution of the utility model operationally, needs as follows for each relevant parameters adjustment:
Air pressure and the temperature of adjustment high-pressure side steam inlet 10 are respectively: 0.1MPa-0.2MPa, 210 DEG C-250 DEG C.
Adjustment high-pressure side steam flow is: be less than or equal to 6000 kgs/hr, namely the maximum value of flow is 6000 kgs/hr.
Air pressure and the temperature of adjustment high-pressure side vapour outlet 30 are respectively: 0.1MPa-0.2MPa, 175 DEG C-185 DEG C.
Air pressure and the temperature of adjustment low pressure end juice vapor inlet 20 are respectively: 0.00MPa-0.03MPa, 92 DEG C-98 DEG C.
Air pressure and the temperature of adjustment low pressure end juice vapour outlet 40 are respectively: 0.00MPa-0.03MPa, 105 DEG C-115 DEG C.
Adjustment low pressure end juice steam flow amount is: be less than or equal to 17000 kgs/hr, namely the maximum value of flow is 17000 kgs/hr.
Existing sugar refinery uses III effect juice steam to boil sugar and does not reach result of use, and III effect juice steam temperature is only 95 DEG C ± about 3, and cause III effect juice steam to boil the sugar time long, flow process is slow.The technical solution of the utility model adopt turbine discharge (enter cooling bucket 51 before waste vapour, temperature 230 DEG C ± 20 DEG C) by heat exchanging apparatus 100, namely steam turbine waste vapour (0.2MPa is adopted, 230 DEG C) as high-end thermal source, by indirect type heat exchanging apparatus 100, evaporation III effect juice steam temperature is risen to 105 DEG C-110 DEG C that meet processing requirement from existing 95 DEG C ± 3 DEG C, and then ensure that boiling the normal III effect juice steam that uses of sugar boils sugar, solving current production technique uses III effect vapour to boil the technical barrier of sugar, shorten flow time, improve heat-economy, reach energy-saving and cost-reducing object.
Per diem squeeze the following parameter that 7500 tons of sugarcanes provide:
1, daily squeezed quantity: 7500 tons (maximum value design)
2, III effect juice steam pressure: 0-0.01MPa
3, III effect juice steam temperature: 95 DEG C ± 3 DEG C
4, exhaust steam main's pressure: 0.15MPa-0.2MPa
5, exhaust steam main's temperature: 230 DEG C ± 20 DEG C
6, methose III effect juice steam caliber size: 900mm
7, methose III effect juice steam steam compares with sugarcane: 5.31%
Calculate methose III effect juice steam hour flux values (maximum value)
7500 tons of sugarcane ÷, 24 hours × 5.31%=16.5 ton/hour
Account can know from technique, it is 16.5 tons/hour that methose extracts III effect evaporating pot juice vapour amount (maximum value), adopt automatic steam of the present utility model to balance temperature elevation system and the temperature of evaporation III effect juice steam and pressure can be brought up to 105 DEG C about-115 DEG C, be equivalent to the parameter level obtaining evaporating I effect juice steam, then clear juice I and II heating and boil sugar and use I, II effect juice steam less, reduce boiler live steam and supplement usage quantity, reach whole sugar refining technology and use juice vapour and heat recuperation, the heat economy object of energy efficiency.
The technical solution of the utility model creates significant effect, greatly improves the heat economy benefit after III effect juice steam temperature, specific as follows:
Learn from above calculating, the III effect juice steam extraction amount about 16.5 tons/hour of existing evaporation area, utilize steam enthalpy entropy to calculate heat-economy, then look into Mollier diagram and obtain:
Promote evaporation III juice stripping temperature 115 DEG C---2698.8kj/kg
Steam turbine waste vapour 0.2MPa, 230 DEG C---2930.2kj/kg (before heat exchange)
Steam turbine waste vapour 0.2MPa, 200 DEG C---2870kj/kg (after heat exchange)
Boiler Steam 2.45MPa, 400 DEG C---3239.29kj/kg
1, Boiler Steam amount (note: calculate by the former evaporation III effect juice steam that can not use) is saved:
16.5t/h × (2698.8kj/kg/3239.29kj/kg)=13.75 ton/hour;
2, improve sugar refining technology efficiency, shorten and boil the sugar time;
4, reduce evaporated final-effect loss to ignore;
5, with boiler efficiency and bagasse combustion heat value, fuel wood doses about 0.45 ton of bagasse produces 1 ton of steam, then
Ton bagasse=6.18,13.75 tons of/hour steam × 0.45 ton bagasse;
6, squeeze and calculated by 120 days in season, by the 1 ton of calculating of 3 tons of bagasse signature coal amounts, coal price 1200 yuan/ton calculating is on average marked in market, can save heat economy loss each squeezing season about:
6.18 tons of bagasse × 24 hour × 120 days=17798 tons bagasses
17798 tons of bagasse ÷, 3 tons of bagasse × 1200 yuan/ton=7,120,000 yuan;
7, thermosteresis calculates: consume steam turbine waste vapour amount 10 tons/hour, steam enthalpy decline 2930.2kj/kg-2870kj/kg=60.2kj/kg per ton, then
10t/h × (60.2kj/kg/3239.29kj/kg)=0.18 ton/hour
0.18 ton/hour × 24 hours × 120 days=518.4 tons bagasses
518.4 tons of bagasse ÷, 3 tons of bagasse × 1200 yuan/ton=210,000 yuan
Direct generation heat economy benefit: 7,120,000 yuan-21 ten thousand yuan=6,910,000 yuan.
The above; be only the utility model preferably embodiment; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; the change that can expect easily or replacement, all should be encompassed within protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion with the protection domain of claims.
Claims (1)
1., for an automatic steam balance heat riser for sugar refining technology, it is characterized in that, comprising:
Heat exchanging apparatus, described heat exchanging apparatus is tube bundle heat exchanger, and described tube bundle heat exchanger is located on III effect juice steam pipeline, and is connected with steam turbine waste vapour pipeline with the second connecting tube by the first connecting tube; Described heat exchanging apparatus is provided with high-pressure side steam inlet, high-pressure side vapour outlet, low pressure end juice vapor inlet and low pressure end juice vapour outlet, wherein, the front-end pipelines that described high-pressure side steam inlet flows into by the first connecting tube and steam turbine waste vapour bucket of lowering the temperature is connected, and the first connecting tube is provided with the first steam flow control valve, the rear end pipeline that described high-pressure side vapour outlet flows out by the second connecting tube and steam turbine waste vapour bucket of lowering the temperature is connected; Described low pressure end juice vapor inlet and low pressure end juice vapour outlet are located on same axis, and the 3rd pipeline be connected with low pressure end juice vapour outlet is provided with the second steam flow control valve; Steam flow control valve, described steam flow control valve is located at steam and is flowed into and flow out on the pipeline of heat exchanging apparatus; PLC, described PLC controls the operation of steam flow control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520003552.8U CN204509362U (en) | 2015-01-05 | 2015-01-05 | A kind of balance of the automatic steam for sugar refining technology heat riser |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520003552.8U CN204509362U (en) | 2015-01-05 | 2015-01-05 | A kind of balance of the automatic steam for sugar refining technology heat riser |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204509362U true CN204509362U (en) | 2015-07-29 |
Family
ID=53707356
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520003552.8U Active CN204509362U (en) | 2015-01-05 | 2015-01-05 | A kind of balance of the automatic steam for sugar refining technology heat riser |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204509362U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104531906A (en) * | 2015-01-05 | 2015-04-22 | 广西南宁富慧达机电有限公司 | Automatic steam balance temperature rise device for sugar production process |
-
2015
- 2015-01-05 CN CN201520003552.8U patent/CN204509362U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104531906A (en) * | 2015-01-05 | 2015-04-22 | 广西南宁富慧达机电有限公司 | Automatic steam balance temperature rise device for sugar production process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107940538A (en) | A kind of classification hold over system and its peak regulating method for cogeneration units | |
| CN107416930B (en) | Multipotency couples seawater desalination system | |
| CN103371716A (en) | Normal pressure steamer | |
| CN207893829U (en) | A kind of classification hold over system for cogeneration units | |
| CN101191699B (en) | Cement residual heat-recovering system and method | |
| CN206449622U (en) | Electric pole type hot-water boiler circulation process system | |
| CN207562379U (en) | A kind of absorption compression heat pump distillation system | |
| CN109441577A (en) | Absorption heat pump cogeneration units recirculated cooling water tower operation method above freezing | |
| CN104531906A (en) | Automatic steam balance temperature rise device for sugar production process | |
| CN204509362U (en) | A kind of balance of the automatic steam for sugar refining technology heat riser | |
| CN104531905A (en) | Automatic steam balance temperature rise system for sugar production process and implement method thereof | |
| CN204509361U (en) | A kind of balance of the automatic steam for sugar refining technology temperature elevation system | |
| CN113280390B (en) | Deep peak regulation heat supply grade improving system and method based on heat pump boosting reheating | |
| CN205957140U (en) | Heating system that heat utilization efficiency is high | |
| CN201852073U (en) | Two-stage flash evaporator for improving utilization efficiency of waste gas in cement waste heat power generation | |
| CN204569884U (en) | A kind of Wort boiling system of reusable edible secondary steam | |
| CN203656895U (en) | Device for preventing low temperature corrosion on coal economizer heating surfaces | |
| CN210069822U (en) | High-pressure high-temperature condensed water flash evaporation recovery system | |
| CN207112762U (en) | Utilize gas turbine electricity/steam co-producing system of smoke discharging residual heat volume increase steam | |
| CN208858422U (en) | Thermal generation unit heat storage type assists peak regulation heating system | |
| CN109296415B (en) | Combined cycle combined cooling heating power unit steam supply superheat degree utilization system | |
| CN203271921U (en) | Combined heat and power closed heat supply system of gas turbine generating set | |
| CN201445816U (en) | Super thickening device | |
| CN105797414A (en) | Industrial waste heat recycling method and device | |
| CN206876003U (en) | Charcoal ink factory's calcining furnace waste heat comprehensive utilization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 530200, 16 emperor street, five elephant Road, Nanning, the Guangxi Zhuang Autonomous Region, Patentee after: Guangxi fuhuida electromechanical Co.,Ltd. Address before: 530200 No. 1119, No. 1 elephant drive, No. five, elephant Road, the Guangxi Zhuang Autonomous Region, Nanning Patentee before: GUANGXI NANNING FUHUIDA ELECTROMECHANICAL Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200429 Address after: No. 102, building B17, Yanxiang Zhigu, No. 7, Nahong Avenue, Jiangnan District, Nanning City, Guangxi Zhuang Autonomous Region Patentee after: Guangxi Feipeng energy conservation and Environmental Protection Technology Co.,Ltd. Address before: 530200, 16 emperor street, five elephant Road, Nanning, the Guangxi Zhuang Autonomous Region, Patentee before: Guangxi fuhuida electromechanical Co.,Ltd. |