CN106390491A - Process system for producing cooling crystallization product with neutralization method - Google Patents

Process system for producing cooling crystallization product with neutralization method Download PDF

Info

Publication number
CN106390491A
CN106390491A CN201610917360.7A CN201610917360A CN106390491A CN 106390491 A CN106390491 A CN 106390491A CN 201610917360 A CN201610917360 A CN 201610917360A CN 106390491 A CN106390491 A CN 106390491A
Authority
CN
China
Prior art keywords
water
liquid
evaporation
unit
sequentially
Prior art date
Application number
CN201610917360.7A
Other languages
Chinese (zh)
Inventor
刘军
侯超
张钰
张俊浩
蔺雪军
Original Assignee
常州博睿杰能环境技术有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 常州博睿杰能环境技术有限公司 filed Critical 常州博睿杰能环境技术有限公司
Priority to CN201610917360.7A priority Critical patent/CN106390491A/en
Publication of CN106390491A publication Critical patent/CN106390491A/en

Links

Classifications

    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/0064Feeding of liquid into an evaporator
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/0094Evaporating with forced circulation
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/28Evaporating with vapour compression
    • B01D1/2803Special features relating to the vapour to be compressed
    • B01D1/2812The vapour is coming from different sources
    • B01D1/2815At least one source is a compressor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/28Evaporating with vapour compression
    • B01D1/2803Special features relating to the vapour to be compressed
    • B01D1/2818Cleaning of the vapour before compression, e.g. demisters, washing of the vapour
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/30Accessories for evaporators ; Constructional details thereof
    • Y02P70/34

Abstract

The invention discloses a process system for producing a cooling crystallization product with a neutralization method. The process system comprises a neutralization synthesis unit, an evaporation and concentration unit, a crystallization unit and a drying unit; the evaporation and concentration unit comprises a separation part, a compression condensation circulation part and a water spraying circulation part; the separation part is used for separating vapor from a raw material solution; the compression condensation circulation part is used for compressing the vapor produced by the separation part into high-temperature high-pressure saturated vapor, and meanwhile, the produced condensed water is cooled and sprayed after preheating the raw material solution through the water spraying circulation part. The invention relates to the process system and gradient utilization of waste heat of a compressor, the secondary vapor, the condensed water and the waste heat of circulation water are all recovered, the comprehensive heat utilization efficiency of the system is remarkably improved, meanwhile, the water is sprayed in an adjustable manner, the insulation efficiency and the volume efficiency of the positive-displacement compressor are improved, the energy consumption per unit of the process system is reduced, and the process system is more energy-saving.

Description

A kind of neutralisation produces the process system of crystallisation by cooling type product

Technical field

The present invention relates to the energy-efficient process system in one of industrial evaporation field, produce particularly to a kind of neutralisation The process system of crystallisation by cooling type product.

Background technology

The consumption of China's energy is concentrated mainly on industrial evaporation operating unit, in medicine, chemical industry, food, environmental protection at present Very big Deng the energy resource consumption in field;Adopting multiple-effect evaporation technology traditional evaporation technology, its floor space is big, high energy consumption more, And adopting steam heating, predominantly coal burning boiler burning is obtained vapor, and its efficiency of combustion is low, sulfide or emitting nitride amount High, CO2 emissions are big, seriously polluted.

CN94111803.7 and CN200810122701.7 individually discloses using steam heating evaporation and concentration, Jin Erleng But crystallization obtains ammonium phosphate, ammonium chloride;CN201110029274.X discloses a kind of low-temperature multiple-effect evaporation crystallization filtering technique side Method, is evaporated, is concentrated using four-effect evaporator device, the method for crystallisation by cooling;CN201210329385.7 discloses one kind With the method for Wet-process Phosphoric Acid Production MAP coproduction N-P binary compound fertilizer, it is evaporated using two-effect evaporation device device, dense Contracting, crystallisation by cooling;CN201320214944.X and CN201310103497.5 discloses a kind of positive displacement compressor MVR heat pump and steams The system of sending out.

Currently existing evaporation, concentration, crystallisation by cooling system exist inefficiency, high energy consumption, system complex, non-science, Still there are the shortcomings such as certain dependence to steam, fail to consider well the exhaust heat stepped utilization of system, cause system comprehensive Close that efficiency of utilization is not high, the problems such as positive displacement compressor is inefficient.

Content of the invention

The technical problem to be solved is:Overcome the shortcomings of that prior art exists, propose one kind and more efficiently save The neutralisation of energy produces the process system of crystallisation by cooling type product, and this system cooling water spray after preheating regulates and controls positive displacement pressure The injection flow rate of contracting machine and injection water temperature, improve adiabatic efficiency and the volumetric efficiency of positive displacement compressor, reduce system unit Power consumption, thus decrease the consumption of vapor and waste heat wastes and carries out energy-conservation.

In order to solve above-mentioned technical problem, the technical scheme is that:A kind of neutralisation produces crystallisation by cooling type product Process system, described process system includes neutralizing synthesis unit, evaporation and concentration unit, crystalline element and drying unit, described Neutralization synthesis unit is connected with evaporation and concentration unit, and evaporation and concentration unit is connected with crystalline element, crystalline element and drying Unit is connected;

Described neutralization synthesis unit is used for input, reaction and the precipitation of raw material;

Described evaporation and concentration unit includes separate section, compression condensation cyclic part and water spray cyclic part, described separation Part is used for separating vapor from material liquid, and described compression condensation part is used for the vapor producing separate section The saturated vapor of boil down to High Temperature High Pressure, the condensed water simultaneously producing completes the preheating to material liquid by cyclic part of spraying water Afterwards, condensed water carries out cooling water spray;

Described crystalline element is used for the material liquid crystallisation by cooling out from evaporation and concentration unit;

Described drying unit is used for for the semi-finished product crystallizing out drying becoming qualified products.

Further, described neutralization synthesis unit includes being sequentially connected raw material input part, neutralization reaction part, precipitation portion Point, wherein part thrown in by raw material is liquid acid or alkali storage tank, and neutralization reaction part is neutralization stirred tank (NT01), precipitation portion It is divided into sedimentation tank (ST01).

Further, described evaporation and concentration unit includes:

Regenerator section, including the feed pump (P01) being sequentially connected, one-level preheater (E01), two grades of preheaters (E02), three The path that level preheater (E03) is constituted;

Concentration cycles part, is sequentially connected composition including heater (E04), gas-liquid separator (F01), circulating pump (P02) Peripheral passage, wherein gas-liquid separator (F01) constitutes separate section, the liquid of the three-level preheater (E03) of regenerator section Outlet is connected with the liquid-inlet of heater (E04) bottom of concentration cycles part;

Compression condensation cyclic part, including positive displacement compressor (C01), second separator (F02), heater (E04), cold Solidifying water pot (V01) is sequentially connected the peripheral passage of composition, the wherein gas outlet of gas-liquid separator (F01) and positive displacement compressor (C01) gas feed connects, and forms the steam of High Temperature High Pressure, heated device (E04) after positive displacement compressor (C01) compression Circulation feed liquid is heated, the condensed water of generation enters condensate water pot (V01), heater (E04) constitutes vapor heating Part;

Water spray cyclic part, including condensate water pot (V01), water jet pump (P05), two grades of preheaters (E02), positive displacement compressions Machine (C01), second separator (F02) are sequentially connected the peripheral passage of composition, improve appearance by adjusting injection flow rate and injection water temperature The adiabatic efficiency of long-pending formula compressor (C01) and volumetric efficiency, second separator (F02) and condensate water pot (V01) are filled by fluid-tight Put and be connected, unnecessary water spray is back to condensate water pot (V01).

Further, described evaporation and concentration unit also includes:

Concentrated solution discharge part, including the circulating line being sequentially connected and discharging pump (P03), discharging pump (P03) and concentration The outlet of the circulating pump (P02) of cyclic part connects;

Condensation water residual heat utilizes part, anti-including the condensate pump (P04) being sequentially connected, three-level preheater (E03), neutralization Answer the path that part (NT01) is constituted, condensate pump (P04) is connected with the outlet of condensate water pot (V01), using condensation water residual heat Heating three-level charging, and condensed water is ultimately discharged into neutralization reaction part (NT01);

Circulating water afterheat recycles part, including circulation water pot (V02), water circulating pump (P06), positive displacement compressor (C01), one-level preheater (E01) is sequentially connected the peripheral passage of composition.

Further, described crystalline element includes crystallizing pond (CP01), and crystallizing pond (CP01) is provided with for by partial mother liquid It is back to the outlet in system, this outlet is connected with feed pump (P01).

Further, described drying unit includes centrifuge (CE01) and/or exsiccator (D01), described centrifuge (CE01) Import be connected with the outlet of crystallizing pond (CP01).

After employing technique scheme, the invention has the advantages that:

1) present invention is additionally arranged separate section, compression condensation cyclic part and water spray circulation portions in evaporation and concentration unit Point, being sprayed water by controllable, effectively adjusting injection flow rate and injection water temperature, thus improve the adiabatic efficiency of positive displacement compressor And volumetric efficiency, reduce system unit power consumption, thus decrease consumption and the waste heat waste of vapor, and then more energy-conservation;

2) present invention out will need with the thin indirect steam of cooling water condensation through volume pressure originally from gas-liquid separator Its temperature is made to increase after contracting, thus realizing the saturated vapor of low temperature, low pressure becomes the saturated vapor of High Temperature High Pressure, and then The material liquid needing to be evaporated can be heated as thermal source again, further up to the purpose of recycling steam;

3) present invention can be full recycled to receive the waste heat using condensed water and recirculated water, significantly improves the synthesis of system Efficiency of utilization;

4) for relatively conventional multiple-effect evaporation and existing MVR thermo-compression evaporation system, using the system more warp of the present invention Ji, energy-conservation, investment cost is moderate, and completely without any type of concurrent heating it is only necessary to electricity can run well completely, can The huge economic benefit of generation, ratio other system more science, more energy-efficient, there is low, working stability of operating cost etc. Advantage.

Brief description

In order to be illustrated more clearly that the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing Have technology description in required use accompanying drawing be briefly described it should be apparent that, drawings in the following description be only this Some embodiments of invention, for those of ordinary skill in the art, on the premise of not paying creative work, acceptable Other accompanying drawings are obtained according to these accompanying drawings.

Fig. 1 is a kind of process system of neutralisation production crystallisation by cooling type product of the present invention;

In figure code name is expressed as follows respectively:

Neutralization reaction part (NT01), sediment fraction (ST01), feed pump (P01), one-level preheater (E01), two grades pre- Hot device (E02), three-level preheater (E03), heater (E04), gas-liquid separator (F01), forced circulation pump (P02), positive displacement Compressor (C01), second separator (F02), vapour source or steam generator (SG01), condensate water pot (V01), water jet pump (P05), discharging pump (P03), condensate pump (P04), circulation water pot (V02), water circulating pump (P06), crystallizing pond (CP01), centrifugation Machine (CE01), exsiccator (D01).

Specific embodiment

In order that present disclosure is easier to be clearly understood, below according to specific embodiment and combine accompanying drawing, right The present invention is described in further detail.

As shown in figure 1, a kind of neutralisation produces the process system of crystallisation by cooling type product, described process system includes neutralizing Synthesis unit, evaporation and concentration unit, crystalline element and drying unit, described neutralization synthesis unit is connected with evaporation and concentration unit Connect, evaporation and concentration unit is connected with crystalline element, and crystalline element is connected with drying unit;

Described neutralization synthesis unit is used for input, reaction and the precipitation of raw material;

Described evaporation and concentration unit includes separate section, compression condensation cyclic part and water spray cyclic part, described separation Part is used for separating vapor from material liquid, and described compression condensation part is used for the vapor producing separate section The saturated vapor of boil down to High Temperature High Pressure, the condensed water simultaneously producing completes the preheating to material liquid by cyclic part of spraying water Afterwards, condensed water carries out cooling water spray;

Described crystalline element is used for the material liquid crystallisation by cooling out from evaporation and concentration unit;

Described drying unit is used for for the semi-finished product crystallizing out drying becoming qualified products.

As shown in figure 1, the raw material input part, neutralization reaction part, heavy that described neutralization synthesis unit includes being sequentially connected It is liquid acid or alkali storage tank that shallow lake part, wherein raw material throw in part, and neutralization reaction part is neutralization stirred tank NT01, precipitation Part is sedimentation tank ST01.

Preferably, as shown in figure 1, described evaporation and concentration unit includes:

Regenerator section, including the feed pump P01 being sequentially connected, one-level preheater E01, two grades of preheater E02, three-level preheatings The path that device E03 is constituted;

Concentration cycles part, is sequentially connected the circulation of composition including heater E04, gas-liquid separator F01, circulating pump P02 Path, wherein gas-liquid separator F01 constitutes separate section, and its internal spin flow separation that carries separates with wire packing, preheating The partial liquid outlet of three-level preheater E03 is connected with the liquid-inlet of the heater E04 bottom of concentration cycles part;

Compression condensation cyclic part, including positive displacement compressor C01, second separator F02, heater E04, condensate water pot V01 is sequentially connected and separates with wire packing inside the peripheral passage of composition, second separator F02, wherein gas-liquid separator F01 Gas outlet be connected with the gas feed of positive displacement compressor C01, through positive displacement compressor C01 compression after formed High Temperature High Pressure Steam, heated device E04 heats to circulation feed liquid, and the condensed water of generation enters condensate water pot V01, heater E04 structure Become vapor heating part, vapour source or steam generator SG01 after second separator F02, right before heater E04 Process system carries out starting preheating;

Water spray cyclic part, including condensate water pot V01, water jet pump P05, two grades of preheater E02, positive displacement compressor C01, Second separator F02 is sequentially connected the peripheral passage of composition, improves positive displacement compressor by adjusting injection flow rate and injection water temperature The adiabatic efficiency of C01 and volumetric efficiency, second separator F02 is connected by liquid seal device with condensate water pot V01, unnecessary water spray It is back to condensate water pot V01.

Preferably, as shown in figure 1, described evaporation and concentration unit also includes:

Concentrated solution discharge part, including the circulating line being sequentially connected and discharging pump P03, discharging pump P03 and concentration cycles The outlet of partial circulating pump P02 connects;

Condensation water residual heat utilizes part, including the condensate pump P04 being sequentially connected, three-level preheater E03, neutralization reaction portion Divide the path that NT01 is constituted, condensate pump P04 is connected with the outlet of condensate water pot V01, grading using condensation water residual heat heating three Material, and condensed water is ultimately discharged into neutralization reaction part NT01;

Circulating water afterheat recycles part, including circulation water pot V02, water circulating pump P06, positive displacement compressor C01, one Level preheater E01 is sequentially connected the peripheral passage of composition.

Alternatively, as shown in figure 1, described crystalline element includes crystallizing pond CP01, crystallizing pond CP01 is provided with for by portion Decomposition mother solution is back to the outlet in system, and this outlet is connected with feed pump P01, and crystallizing pond can be arranged as required to several, , crystallizing pond can be natural cooling crystallization or water cooling crystallization to the present embodiment taking a crystallizing pond as a example.

Alternatively, as shown in figure 1, described drying unit includes the centrifuge CE01 being sequentially connected and exsiccator D01, described The import of centrifuge CE01 is connected with the outlet of crystallizing pond CP01;Only carry out centrifugation also dependent on needs from centrifuge CE01 dry Dry, finally give product, packed.

In the present embodiment, it is further described with raw material liq nitric acid and solid sodium carbonate:

Press 2 with nitric acid and sodium carbonate:1 ratio is thrown to neutralization stirred tank NT01 and is reacted, using smoke absorption Process big calorimetric and the fog that reaction produces, sediment fraction is sedimentation tank ST01, need to carry out because sodium carbonate is contained within impurity Precipitation, reacted sodium nitrate solution is passed through sedimentation tank, is precipitated, understand some ferrous carbonate and precipitate, and Part nitric acid sodium crystal.

Sodium nitrate light green mother solution (supernatant) after precipitation passes sequentially through one-level preheater through feed pump P01 After E01, two grades of preheater E02, three-level preheater E03 are preheated, enter forced circulation pump P02 import, with circulation fluid Enter heater E04, carry out heating evaporation, forced circulation pump P02 passes through frequency conversion control circulating load size;From heater E04 pipe Journey gas-liquid mixture out enters gas-liquid separator F01 and carries out cyclonic separation, subsequently secondary after wire packing separates Steam enters positive displacement compressor C01 and is compressed, and regulates and controls optimal injection flow rate simultaneously and injection water temperature is sprayed water, unnecessary water spray Condensate water pot V01 is back to by the liquid seal device being connected between second separator F02 and condensate water pot V01;Steam after compression Vapour pass through the wire packing that carries inside second separator F02 be segregated into heater E04 shell side circulation fluid is carried out heat cold Solidifying, condensed water is constantly collected in condensate water pot V01;Most of condensed water is completed by condensate pump P04, three-level preheater E03 Condensation water residual heat utilizes, and enters neutralization reaction part NT01 and re-uses, and condensation water residual heat is mainly used in heating three-level charging;Few Partial condensation water carries out water spray regulation and control by water jet pump P05, two grades of preheater E02 to positive displacement compressor C01;Recirculated water is main Recirculated water is completed by the circulation water pot V02 that is sequentially connected, water circulating pump P06, positive displacement compressor C01, one-level preheater E01 UTILIZATION OF VESIDUAL HEAT IN, circulating water afterheat is mainly used in heating one-level charging.

The continuous circulating and evaporating of concentrated solution concentrates, and after boiling point temperature rise reaches 15~18 degree, enters through circulating line, discharging pump P03 Row continues discharge, enters crystallizing pond CP01, herein for natural wind crystallisation by cooling, subsequently carries out centrifugal drying, finally give nitric acid Sodium product, is packed, and part sodium nitrate mother liquor reflux again evaporates to internal system, concentrates.If two crystallizing ponds of setting, two Individual crystallizing pond switches over crystallization.

The present invention is additionally arranged separate section, compression condensation cyclic part and water spray cyclic part in evaporation and concentration unit, Being sprayed water by controllable, effectively adjusting injection flow rate and injection water temperature, thus improve the adiabatic efficiency of positive displacement compressor C01 And volumetric efficiency, reduce system unit power consumption, thus decrease consumption and the waste heat waste of vapor, and then more energy-conservation.

The present invention out will need with the thin indirect steam of cooling water condensation through volume pressure originally from gas-liquid separator F01 Its temperature is made to increase after contracting, thus realizing the saturated vapor of low temperature, low pressure becomes the saturated vapor of High Temperature High Pressure, and then The material liquid needing to be evaporated can be heated as thermal source again, further up to the purpose of recycling steam.

The present invention can be full recycled to receive the waste heat using condensed water and recirculated water, significantly improves the Thermal Synthetic of system Utilization ratio.

For relatively conventional multiple-effect evaporation and existing MVR thermo-compression evaporation system, using the system of the present invention more economical, Energy-conservation, investment cost is moderate, and completely without any type of concurrent heating it is only necessary to electricity can run well completely, can produce The huge economic benefit of life, ratio other system more science, more energy-efficient, there is low, working stability of operating cost etc. excellent Point.

The present invention is applied to the salt product that the reaction of acid-base neutralization method generates, and it belongs to the material of crystallisation by cooling process, As nitrate, sulfate, fluosilicate etc..The present invention relates to the exhaust heat stepped utilization of process system and compressor, all reclaim The waste heat of indirect steam, condensed water and recirculated water, significantly improves the comprehensive efficiency of utilization of system, passes through controllable simultaneously Water spray, improves adiabatic efficiency and the volumetric efficiency of positive displacement compressor, reduces process system unit energy consumption.

Particular embodiments described above, to present invention solves the technical problem that, technical scheme and beneficial effect carry out Further describe, be should be understood that the specific embodiment that the foregoing is only the present invention, be not limited to this Invention, all any modification, equivalent substitution and improvement within the spirit and principles in the present invention, done etc., should be included in this Within bright protection domain.

Claims (6)

1. a kind of neutralisation produce crystallisation by cooling type product process system it is characterised in that:Described process system includes neutralizing Synthesis unit, evaporation and concentration unit, crystalline element and drying unit, described neutralization synthesis unit is connected with evaporation and concentration unit Connect, evaporation and concentration unit is connected with crystalline element, and crystalline element is connected with drying unit;
Described neutralization synthesis unit is used for input, reaction and the precipitation of raw material;
Described evaporation and concentration unit includes separate section, compression condensation cyclic part and water spray cyclic part, described separate section For separating vapor from material liquid, the vapor that described compression condensation part is used for producing separate section compresses For the saturated vapor of High Temperature High Pressure, the condensed water simultaneously producing is after cyclic part of spraying water completes the preheating to material liquid, cold Solidifying water carries out cooling water spray;
Described crystalline element is used for the material liquid crystallisation by cooling out from evaporation and concentration unit;
Described drying unit is used for for the semi-finished product crystallizing out drying becoming qualified products.
2. a kind of neutralisation according to claim 1 produce crystallisation by cooling type product process system it is characterised in that:Institute State the raw material input part that neutralization synthesis unit includes being sequentially connected, neutralization reaction part, sediment fraction, wherein raw material input portion It is divided into liquid acid or alkali storage tank, neutralization reaction part is neutralization stirred tank (NT01), sediment fraction is sedimentation tank (ST01).
3. a kind of neutralisation according to claim 2 produces the process system of crystallisation by cooling type product it is characterised in that institute State evaporation and concentration unit to include:
Regenerator section, pre- including the feed pump (P01) being sequentially connected, one-level preheater (E01), two grades of preheaters (E02), three-levels The path that hot device (E03) is constituted;
Concentration cycles part, is sequentially connected following of composition including heater (E04), gas-liquid separator (F01), circulating pump (P02) Ring path, wherein gas-liquid separator (F01) constitute separate section, the liquid outlet of the three-level preheater (E03) of regenerator section It is connected with the liquid-inlet of heater (E04) bottom of concentration cycles part;
Compression condensation cyclic part, including positive displacement compressor (C01), second separator (F02), heater (E04), condensed water Tank (V01) is sequentially connected the peripheral passage of composition, the wherein gas outlet of gas-liquid separator (F01) and positive displacement compressor (C01) gas feed connects, and forms the steam of High Temperature High Pressure, heated device (E04) after positive displacement compressor (C01) compression Circulation feed liquid is heated, the condensed water of generation enters condensate water pot (V01), heater (E04) constitutes vapor heating Part;
Water spray cyclic part, including condensate water pot (V01), water jet pump (P05), two grades of preheaters (E02), positive displacement compressors (C01), second separator (F02) is sequentially connected the peripheral passage of composition, improves volume by adjusting injection flow rate and injection water temperature The adiabatic efficiency of formula compressor (C01) and volumetric efficiency, second separator (F02) and condensate water pot (V01) pass through liquid seal device It is connected, unnecessary water spray is back to condensate water pot (V01).
4. a kind of neutralisation according to claim 3 produces the process system of crystallisation by cooling type product it is characterised in that institute State evaporation and concentration unit also to include:
Concentrated solution discharge part, including the circulating line being sequentially connected and discharging pump (P03), discharging pump (P03) and concentration cycles The outlet of partial circulating pump (P02) connects;
Condensation water residual heat utilizes part, including the condensate pump (P04) being sequentially connected, three-level preheater (E03), neutralization reaction portion Divide the path that (NT01) is constituted, condensate pump (P04) is connected with the outlet of condensate water pot (V01), using condensation water residual heat heating Three-level feeds, and condensed water is ultimately discharged into neutralization reaction part (NT01);
Circulating water afterheat recycles part, including circulation water pot (V02), water circulating pump (P06), positive displacement compressor (C01), One-level preheater (E01) is sequentially connected the peripheral passage of composition.
5. a kind of neutralisation according to claim 4 produce crystallisation by cooling type product process system it is characterised in that:Institute State crystalline element and include crystallizing pond (CP01), crystallizing pond (CP01) is provided with for partial mother liquid is back to going out in system Mouthful, this outlet is connected with feed pump (P01).
6. a kind of neutralisation according to claim 5 produces the process system of crystallisation by cooling type product it is characterised in that institute State drying unit and include centrifuge (CE01) and/or exsiccator (D01), the import of described centrifuge (CE01) and crystallizing pond (CP01) outlet connects.
CN201610917360.7A 2016-10-20 2016-10-20 Process system for producing cooling crystallization product with neutralization method CN106390491A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610917360.7A CN106390491A (en) 2016-10-20 2016-10-20 Process system for producing cooling crystallization product with neutralization method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610917360.7A CN106390491A (en) 2016-10-20 2016-10-20 Process system for producing cooling crystallization product with neutralization method

Publications (1)

Publication Number Publication Date
CN106390491A true CN106390491A (en) 2017-02-15

Family

ID=58013534

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610917360.7A CN106390491A (en) 2016-10-20 2016-10-20 Process system for producing cooling crystallization product with neutralization method

Country Status (1)

Country Link
CN (1) CN106390491A (en)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102817849A (en) * 2011-06-07 2012-12-12 株式会社神户制钢所 Water spray type steam compressor
CN103241749A (en) * 2013-05-10 2013-08-14 甘肃蓝科石化高新装备股份有限公司 Anhydrous sodium sulfate production system and production method
CN103785185A (en) * 2014-02-11 2014-05-14 莱州市新力复合材料有限公司 Evaporation and concentration system and method
CN104069642A (en) * 2013-03-28 2014-10-01 中国科学院理化技术研究所 Positive-displacement compressor MVR heat pump evaporation system with adjustable pressure ratio working condition
CN104707349A (en) * 2015-02-05 2015-06-17 中国科学院理化技术研究所 Plate evaporator type MVC heat pump evaporation system
CN105031965A (en) * 2015-07-22 2015-11-11 深圳市捷晶能源科技有限公司 Zero-emission evaporation and crystallization device
CN206152365U (en) * 2016-10-20 2017-05-10 常州博睿杰能环境技术有限公司 Process systems of neutralization production cooling crystallization type product

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102817849A (en) * 2011-06-07 2012-12-12 株式会社神户制钢所 Water spray type steam compressor
CN104069642A (en) * 2013-03-28 2014-10-01 中国科学院理化技术研究所 Positive-displacement compressor MVR heat pump evaporation system with adjustable pressure ratio working condition
CN103241749A (en) * 2013-05-10 2013-08-14 甘肃蓝科石化高新装备股份有限公司 Anhydrous sodium sulfate production system and production method
CN103785185A (en) * 2014-02-11 2014-05-14 莱州市新力复合材料有限公司 Evaporation and concentration system and method
CN104707349A (en) * 2015-02-05 2015-06-17 中国科学院理化技术研究所 Plate evaporator type MVC heat pump evaporation system
CN105031965A (en) * 2015-07-22 2015-11-11 深圳市捷晶能源科技有限公司 Zero-emission evaporation and crystallization device
CN206152365U (en) * 2016-10-20 2017-05-10 常州博睿杰能环境技术有限公司 Process systems of neutralization production cooling crystallization type product

Similar Documents

Publication Publication Date Title
CN103007553B (en) A kind of function of mechanical steam recompression continuous evaporative crystallization system and method
CN101544437B (en) Process method for recovering ammonium chloride and sodium chloride from waste water containing ammonium chloride and sodium chloride
CN103203116A (en) MVR (Mechanical Vapor Recompression) continuous evaporative crystallization system and continuous evaporative crystallization method
CN100497190C (en) Low-position heat energy spray evaporation-multiple-effect distillation seawater desalination method and device
CN103768808B (en) Some vapor recompression evaporation concentration system and method
CN103265089B (en) High temperature high efficiency multi-effect seawater distillation desalination apparatus and method
CN101968299B (en) Method for drying materials by utilizing superheated steam
CN201492958U (en) Triple-effect four-body counter-flow evaporator
CN102616973B (en) Method and device for processing high-saline organic wastewater
CN103539132B (en) The method of Neutral ammonium fluoride is reclaimed from potassium felspar sand gas phase adsorption liquid
CN101319828A (en) Absorption type refrigeration and power combined circulating system
CN102225240B (en) Concentration method based on combination of titanium liquid film evaporation and multilevel flash evaporation
CN1323032C (en) Apparatus of combined solar energy heat pump for desaltination of sea water
CN204251456U (en) Evaporative crystallization is adopted to realize the device of Coal Chemical Industry height strong brine recycling
CN102603023B (en) Method and equipment for carrying out evaporation-concentration treatment on saline water by utilizing solar energy and air
CN102145912B (en) Process for preparing calcium chloride solution by utilizing ammonia soda filtration mother liquor
CN103819041A (en) Method for concentrating high-salinity wastewater at low temperature
CN105923676B (en) High-efficiency solar sea water desalination and air conditioner refrigerating cooperation method and system
CN101549929B (en) Method for distilling absorption type negative-pressure thermal cycle coking wastewater
CN102343162B (en) Energy-saving evaporating process and equipment for L-phenylalanine brine solution
CN103161528B (en) Work and coldness co-production system and method of recovering working medium effective ingredient refrigeration
CN202590405U (en) Triple effect concentration evaporator
CN102336448B (en) Saline treatment system and method
CN204417273U (en) Phosphorus-containing wastewater special processor in phosphorous chemical industry production
CN102797524B (en) Medium-and-low-temperature waste-heat utilization cooling/power combination system

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication
RJ01 Rejection of invention patent application after publication

Application publication date: 20170215