CN103830921A - System and technology for evaporation concentration of extraction water - Google Patents
System and technology for evaporation concentration of extraction water Download PDFInfo
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- CN103830921A CN103830921A CN201310642651.6A CN201310642651A CN103830921A CN 103830921 A CN103830921 A CN 103830921A CN 201310642651 A CN201310642651 A CN 201310642651A CN 103830921 A CN103830921 A CN 103830921A
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Abstract
The invention provides a system and a technology for evaporation concentration of extraction water. The system for evaporation concentration of extraction water comprises a plate-type heat exchanger set, a primary falling-film evaporator, a secondary falling-film evaporator, a tertiary falling-film evaporator, a cyclone separator, a steam tower, a steam condenser, a condensate collection tank set, a centrifugal compressor set, a concentrate storage tank and a condensate storage tank. The system realizes system pressure automatically-controlled adjustment by discharge of redundant steam to the steam condenser or supplement of steam from the steam condenser. The system utilizes system internal self-circulation heating to replace supplied steam heating in production but in an operation initial-stage so that energy consumption is greatly reduced, high economic benefit is obtained and a production cost is reduced.
Description
[technical field]
The present invention relates to a kind of extraction water evaporation concentration system and technique thereof.
[background technology]
In extraction water, generally contain part producing raw material, in order to realize the reasonable utilization of resource, avoid waste and reduce production costs, generally the raw materials for production in extraction water need be carried out to evaporation and concentration recovery.
Old traditional evaporation technology is to produce steam with coal-fired steam boiler heating steam condensed water to provide thermal source, average one tonne of fire coal approximately can be produced 7 tonnes of 1.0Mpa steams, and triple effect steam efficiency 250% is for calculating benchmark, when evaporated water reaches production capacity 26, when 000kg/hr, per hour need consumed 10.4 tonnes of 1.0Mpa steams, needs bituminous coal 1485.7kg/hr, need consume coal-fired 35 every day, 657kg, the 1 year needs 13,014 that turns round, the bituminous coal of 732kg.With 900 yuan of calculating of per metric ton bituminous coal, bituminous coal cost is 32,091 yuan/day, the bituminous coal of 1,171.3371 ten thousand yuan of the 1 year needs of turning round.Row's carbon amount of burning 1kg bituminous coal output 2.62kg.As use the annual row's carbon amount of traditional vapo(u)rization system will be up to 34,239,912kg.
Due to above-mentioned shortcoming, we intend adopting novel energy-conserving to subtract charcoal extraction water evaporating and concentrating process technology, to reduce row's carbon amount and production cost.
[summary of the invention]
One of the technical problem to be solved in the present invention problem, is to provide a kind of extraction water evaporation concentration system, and its evaporation and concentration is effective, can also reduce row's carbon amount and production cost simultaneously.
The present invention is one of above-mentioned technical problem realizing like this:
A kind of extraction water evaporation concentration system, described extraction water evaporation concentration system comprises a plate type heat exchanger group, an effect falling film evaporator, two effect falling film evaporators, triple effect falling film evaporator, a cyclone separator, turret, stram condenser, condensed fluid collection tank group, Systems of Centrifugal Compressor Unit, concentrate storage tank, condensate liquid storage tank;
Described plate type heat exchanger group is connected with an effect falling film evaporator, condensate liquid storage tank respectively, a described effect falling film evaporator bottom is connected to respectively an effect falling film evaporator and two effect falling film evaporator tops by the first circulating pump, described two effect falling film evaporator bottoms are connected to two effect falling film evaporator tops by one second circulating pump and one the 3rd circulating pump respectively, described two effect falling film evaporator bottoms are also connected to triple effect falling film evaporator top by the 4th circulating pump, and described triple effect falling film evaporator is also connected with concentrate storage tank;
A described effect falling film evaporator is connected with described cyclone separator, and described two effect falling film evaporators, triple effect falling film evaporator are connected with turret respectively, and described turret top is also provided with a sprinkling equipment;
The top of described cyclone separator is connected with two effect falling film evaporators and stram condenser respectively, and described stram condenser is connected with condensed fluid collection tank group, and described condensed fluid collection tank group is connected with plate type heat exchanger group;
The import of described Systems of Centrifugal Compressor Unit is connected with turret top, and the outlet of described Systems of Centrifugal Compressor Unit is connected with an effect falling film evaporator, triple effect falling film evaporator.
Further, described cyclone separator bottom is also connected with the first circulating pump; The bottom of described turret is connected with the second circulating pump.
Further, described sprinkling equipment is connected with plate type heat exchanger group.
Further, described Systems of Centrifugal Compressor Unit is also connected with condensed fluid collection tank group.
Further, the bottom of a described effect falling film evaporator, triple effect falling film evaporator is all connected to two effect falling film evaporators, and the bottom of described two effect falling film evaporators is connected to condensed fluid collection tank group.
Two of the technical problem to be solved in the present invention problem, is to provide a kind of extraction water evaporating and concentrating process, and its evaporation and concentration is effective, can also reduce row's carbon amount and production cost simultaneously.
The present invention is two of the above-mentioned technical problem that realizes like this:
A kind of extraction water evaporating and concentrating process, described processing step is as follows:
After step 20, extraction water enter an effect falling film evaporator, warp is by the first circulating pump forced circulation, and be concentrated to predetermined concentration with the steam under pressure heat exchange heating that Systems of Centrifugal Compressor Unit produces, be transported to again in two effect falling film evaporators, simultaneously after heating, moisture evaporation in extraction water produces secondary steam, secondary steam enters cyclone separator and carries out vapor-liquid separation, and the liquid after separation is collected the first pump entry in cyclone separator bottom;
Extraction water in step 30, two effect falling film evaporators is carried out forced circulation through the second circulating pump and the 3rd circulating pump, and be concentrated to predetermined concentration with the secondary steam heat exchange heating entering in the cyclone separator of two effect falling film evaporators, send into again triple effect falling film evaporator, and the steam that the evaporation of moisture in extraction water produces enters F02 steam tower;
Extraction water in step 40, triple effect falling film evaporator is through the 4th circulating pump forced circulation, and carries out heat exchange heating with Systems of Centrifugal Compressor Unit steam under pressure and be concentrated to predetermined concentration, after be transported to concentrate storage tank and deposit;
In two effect falling film evaporators and triple effect falling film evaporator extraction water, all entered steam tower by the steam that transpiring moisture produced, and through condensed water hydro-peening, the material monomer of taking out of to wash out steam, steam after cleaning enters Systems of Centrifugal Compressor Unit pressurization, and the steam after pressurization will be supplied with extraction water evaporation concentration system as evaporation thermal source;
The condensed water accumulating in Systems of Centrifugal Compressor Unit can be delivered to condensation water collection tank group, the condensed water that extraction water evaporation concentration system inner vapor produces after heat exchange also will be collected in condensation water collection tank group, a condensed water part is after plate type heat exchanger group is carried out heat exchange, be re-used as steam tower hydro-peening water, all the other condensed waters will be collected condensation water collection storage tank;
Extraction water evaporation concentration system pressure adopts automatically and controls, can be by unnecessary vapor discharge to vapour condenser or supplementary steam with regulating system internal pressure.
Tool of the present invention has the following advantages:
System pressure of the present invention adopts automatically to be controlled unnecessary vapor discharge to vapour condenser or supplements the pressure of steam with regulating system from vapour condenser again, extraction water evaporation concentration system of the present invention heats up heating except initial stage running needs to use external steam, in production process, all need not use external steam, internal system self-loopa heating, significantly reduce energy consumption, there is height economic benefit, can also reduce production costs.
When extraction water production capacity is during at 26,000kg/hr, utilize system of the present invention only to need to use electric power 578kw/hr, with 0.65 yuan of calculating of the every degree electricity of commercial power, the cost of annual power drain is 3,234,192 yuan, save cost payout and can reach 8,479,179 yuan/year, row's carbon amount is 4,236,686kg/ (every degree electricity row carbon amount is 0.904kg), reduces 30,003 every year, row's carbon amount of 226kg, can reduce the pollution to environment greatly.
[accompanying drawing explanation]
The present invention is further illustrated in conjunction with the embodiments with reference to the accompanying drawings.
Fig. 1 is system architecture schematic diagram of the present invention.
[specific embodiment]
Referring to Fig. 1 is described in detail embodiments of the invention.
As shown in Figure 1, the present invention relates to a kind of extraction water evaporation concentration system, described extraction water evaporation concentration system comprises a plate type heat exchanger group 1, an effect falling film evaporator 2, two effect falling film evaporators 3, triple effect falling film evaporator 4, a cyclone separator 5, turret 6, stram condenser 7, condensed fluid collection tank group 8, Systems of Centrifugal Compressor Unit 9, concentrate storage tank 10, condensate liquid storage tank 11;
Described plate type heat exchanger group 1 is connected with an effect falling film evaporator 2, condensate liquid storage tank 11 respectively, described effect falling film evaporator 2 bottoms are connected to respectively an effect falling film evaporator 2 and two effect falling film evaporator 3 tops by the first circulating pump 12, described two effect falling film evaporator 3 bottoms are connected to two effect falling film evaporator 3 tops by one second circulating pump 13 and one the 3rd circulating pump 14 respectively, described two effect falling film evaporator 3 bottoms are also connected to triple effect falling film evaporator 4 tops by the 4th circulating pump 15, and described triple effect falling film evaporator 4 is also connected with concentrate storage tank 10;
A described effect falling film evaporator 2 is connected with described cyclone separator 5, and described two effect falling film evaporators 3, triple effect falling film evaporator 4 are connected with turret 6 respectively, and described turret 6 tops are also provided with a sprinkling equipment (not shown);
The top of described cyclone separator 5 is connected with two effect falling film evaporators 3 and stram condenser 7 respectively, and described stram condenser 7 is connected with condensed fluid collection tank group 8, and described condensed fluid collection tank group 8 is connected with plate type heat exchanger group 1;
The import of described Systems of Centrifugal Compressor Unit 9 is connected with turret 6 tops, and the outlet of described Systems of Centrifugal Compressor Unit 9 is connected with an effect falling film evaporator 2, triple effect falling film evaporator 3.
Described cyclone separator 5 bottoms are also connected with the first circulating pump 12; The bottom of described turret 6 is connected with the second circulating pump 13.
Described sprinkling equipment is connected with plate type heat exchanger group 1.
Described Systems of Centrifugal Compressor Unit 9 is also connected with condensed fluid collection tank group 8.
The bottom of a described effect falling film evaporator 2, triple effect falling film evaporator 4 is all connected to two effect falling film evaporators 3, and the bottom of described two effect falling film evaporators 3 is connected to condensed fluid collection tank group 8.
The invention still further relates to a kind of extraction water evaporating and concentrating process, described processing step is as follows:
Step 20, extraction water enter after an effect falling film evaporator 2 via the first circulating pump 12 forced circulation, and be concentrated to predetermined concentration with the steam under pressure heat exchange heating that Systems of Centrifugal Compressor Unit 9 produces, be transported to again in two effect falling film evaporators 3, simultaneously after heating, moisture evaporation in extraction water produces secondary steam, secondary steam enters cyclone separator 5 and carries out vapor-liquid separation, the liquid after separation at the bottom of cyclone separator 5 collect the first circulating pump 12 entrances;
Extraction water in step 30, two effect falling film evaporators 3 is carried out forced circulation through the second circulating pump 13 and the 3rd circulating pump 14, and be concentrated to predetermined concentration with the secondary steam heat exchange heating entering in the cyclone separator 5 of two effect falling film evaporators 3, send into again triple effect falling film evaporator 4, and the steam that the evaporation of moisture in extraction water produces enters steam tower 6;
Extraction water in step 40, triple effect falling film evaporator 4 is through the 4th circulating pump 15 forced circulation, and carries out heat exchange heating with Systems of Centrifugal Compressor Unit 9 steams under pressure and be concentrated to predetermined concentration, after be transported to concentrate storage tank 10 and deposit;
In two effect falling film evaporators 3 and triple effect falling film evaporator 4 extraction water, all entered steam tower 6 by the steam that transpiring moisture produced, and through condensed water hydro-peening, the material monomer of taking out of to wash out steam, steam after cleaning enters Systems of Centrifugal Compressor Unit 9 and pressurizes, and the steam after pressurization will be supplied with extraction water evaporation concentration system as evaporation thermal source;
In Systems of Centrifugal Compressor Unit 9, the condensed water of accumulation can be delivered to condensation water collection tank group 8, the condensed water that extraction water evaporation concentration system inner vapor produces after heat exchange also will be collected in condensation water collection tank group 8, a condensed water part is carried out after heat exchange through plate type heat exchanger group 1, be re-used as steam tower 6 hydro-peening waters, all the other condensed waters will be collected condensation water collection storage tank 11;
Extraction water evaporation concentration system pressure adopts automatically and controls, can be by unnecessary vapor discharge to vapour condenser 7 or supplementary steam with regulating system internal pressure.
Internal system of the present invention has certain pressure, and therefore condensed water is actual in the steam after pressurization, has higher temperature.
Original content be 6.5% caprolactam extraction water after the evaporation and concentration of system of the present invention, can be concentrated into concentration and be 70% caprolactam extraction water, therefore evaporation and concentration of the present invention is effective.
System pressure of the present invention adopts automatically to be controlled unnecessary vapor discharge to vapour condenser or supplements the pressure of steam with regulating system from vapour condenser again, extraction water evaporation concentration system of the present invention heats up heating except initial stage running needs to use external steam, in production process, all need not use external steam, internal system self-loopa heating, significantly reduce energy consumption, there is height economic benefit, can also reduce production costs.
When extraction water production capacity is during at 26,000kg/hr, utilize system of the present invention only to need to use electric power 578kw/hr, with 0.65 yuan of calculating of the every degree electricity of commercial power, the cost of annual power drain is 3,234,192 yuan, save cost payout and can reach 8,479,179 yuan/year, row's carbon amount is 4,236,686kg/ (every degree electricity row carbon amount is 0.904kg), reduces 30,003 every year, row's carbon amount of 226kg, can reduce the pollution to environment greatly.
Although more than described the specific embodiment of the present invention; but being familiar with those skilled in the art is to be understood that; our described specific embodiment is illustrative; rather than for the restriction to scope of the present invention; those of ordinary skill in the art are in equivalent modification and the variation done according to spirit of the present invention, all should be encompassed in the scope that claim of the present invention protects.
Claims (6)
1. an extraction water evaporation concentration system, is characterized in that: described extraction water evaporation concentration system comprises a plate type heat exchanger group, an effect falling film evaporator, two effect falling film evaporators, triple effect falling film evaporator, a cyclone separator, turret, stram condenser, condensed fluid collection tank group, Systems of Centrifugal Compressor Unit, concentrate storage tank, condensate liquid storage tank;
Described plate type heat exchanger group is connected with an effect falling film evaporator, condensate liquid storage tank respectively, a described effect falling film evaporator bottom is connected to respectively an effect falling film evaporator and two effect falling film evaporator tops by the first circulating pump, described two effect falling film evaporator bottoms are connected to two effect falling film evaporator tops by one second circulating pump and one the 3rd circulating pump respectively, described two effect falling film evaporator bottoms are also connected to triple effect falling film evaporator top by the 4th circulating pump, and described triple effect falling film evaporator is also connected with concentrate storage tank;
A described effect falling film evaporator is connected with described cyclone separator, and described two effect falling film evaporators, triple effect falling film evaporator are connected with turret respectively, and described turret top is also provided with a sprinkling equipment;
The top of described cyclone separator is connected with two effect falling film evaporators and stram condenser respectively, and described stram condenser is connected with condensed fluid collection tank group, and described condensed fluid collection tank group is connected with plate type heat exchanger group;
The import of described Systems of Centrifugal Compressor Unit is connected with turret top, and the outlet of described Systems of Centrifugal Compressor Unit is connected with an effect falling film evaporator, triple effect falling film evaporator.
2. a kind of extraction water evaporation concentration system according to claim 1, is characterized in that: described cyclone separator bottom is also connected with the first circulating pump; The bottom of described turret is connected with the second circulating pump.
3. a kind of extraction water evaporation concentration system according to claim 1, is characterized in that: described sprinkling equipment is connected with plate type heat exchanger group.
4. a kind of extraction water evaporation concentration system according to claim 1, is characterized in that: described Systems of Centrifugal Compressor Unit is also connected with condensed fluid collection tank group.
5. a kind of extraction water evaporation concentration system according to claim 1, it is characterized in that: the bottom of a described effect falling film evaporator, triple effect falling film evaporator is all connected to two effect falling film evaporators, and the bottom of described two effect falling film evaporators is connected to condensed fluid collection tank group.
6. an extraction water evaporating and concentrating process, is characterized in that: described processing step is as follows:
Step 10, low-concentration caprolactam extraction water is delivered into plate type heat exchanger group, extraction water, via plate type heat exchanger group and the heat exchange of steam condensing water, utilizes the used heat of steam condensing water to improve the temperature of extraction water as thermal source;
After step 20, extraction water enter an effect falling film evaporator, warp is by the first circulating pump forced circulation, and be concentrated to predetermined concentration with the steam under pressure heat exchange heating that Systems of Centrifugal Compressor Unit produces, be transported to again in two effect falling film evaporators, simultaneously after heating, moisture evaporation in extraction water produces secondary steam, secondary steam enters cyclone separator and carries out vapor-liquid separation, and the liquid after separation is collected the first pump entry in cyclone separator bottom;
Extraction water in step 30, two effect falling film evaporators is carried out forced circulation through the second circulating pump and the 3rd circulating pump, and be concentrated to predetermined concentration with the secondary steam heat exchange heating entering in the cyclone separator of two effect falling film evaporators, send into again triple effect falling film evaporator, and the steam that the evaporation of moisture in extraction water produces enters F02 steam tower;
Extraction water in step 40, triple effect falling film evaporator is through the 4th circulating pump forced circulation, and carries out heat exchange heating with Systems of Centrifugal Compressor Unit steam under pressure and be concentrated to predetermined concentration, after be transported to concentrate storage tank and deposit;
In two effect falling film evaporators and triple effect falling film evaporator extraction water, all entered steam tower by the steam that transpiring moisture produced, and through condensed water hydro-peening, the material monomer of taking out of to wash out steam, steam after cleaning enters Systems of Centrifugal Compressor Unit pressurization, and the steam after pressurization will be supplied with extraction water evaporation concentration system as evaporation thermal source;
The condensed water accumulating in Systems of Centrifugal Compressor Unit can be delivered to condensation water collection tank group, the condensed water that extraction water evaporation concentration system inner vapor produces after heat exchange also will be collected in condensation water collection tank group, a condensed water part is after plate type heat exchanger group is carried out heat exchange, be re-used as steam tower hydro-peening water, all the other condensed waters will be collected condensation water collection storage tank;
Extraction water evaporation concentration system pressure adopts automatically and controls, can be by unnecessary vapor discharge to vapour condenser or supplementary steam with regulating system internal pressure.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104826348A (en) * | 2015-04-13 | 2015-08-12 | 铜仁学院 | Extraction mixed liquor treatment method by recycling steam condensate waste heat |
| CN104892479A (en) * | 2014-10-13 | 2015-09-09 | 江苏弘盛新材料股份有限公司 | Caprolactam monomer recycling system |
| CN105498260A (en) * | 2015-12-01 | 2016-04-20 | 北京三联虹普新合纤技术服务股份有限公司 | High-efficiency and energy-saving caprolactam recovery technology |
| CN105858767A (en) * | 2016-06-16 | 2016-08-17 | 恒天中纤纺化无锡有限公司 | Nylon-6 chip monomer water recovery system |
| CN106068149A (en) * | 2016-01-18 | 2016-11-02 | 江门市佰川环境科技有限公司 | A kind of economic benefits and social benefits cross-flow MVR evaporation concentration system |
| CN109381879A (en) * | 2018-12-26 | 2019-02-26 | 郑州博大浓缩干燥设备有限公司 | Aluminium polychloride production evaporation and concentration spray drying system |
| CN109400766A (en) * | 2018-12-29 | 2019-03-01 | 福建三农新材料有限责任公司 | A kind of super low concentration PTFE dispersion emulsion concentration systems |
| CN116658881A (en) * | 2023-07-26 | 2023-08-29 | 上海优华系统集成技术股份有限公司 | Residual heat steam generating system |
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| CN109381879A (en) * | 2018-12-26 | 2019-02-26 | 郑州博大浓缩干燥设备有限公司 | Aluminium polychloride production evaporation and concentration spray drying system |
| CN109400766A (en) * | 2018-12-29 | 2019-03-01 | 福建三农新材料有限责任公司 | A kind of super low concentration PTFE dispersion emulsion concentration systems |
| CN116658881A (en) * | 2023-07-26 | 2023-08-29 | 上海优华系统集成技术股份有限公司 | Residual heat steam generating system |
| CN116658881B (en) * | 2023-07-26 | 2023-09-26 | 上海优华系统集成技术股份有限公司 | Residual heat steam generating system |
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Application publication date: 20140604 |