CN106277115B - A kind of saline sewage crystallizing evaporator, purification system and purification process - Google Patents
A kind of saline sewage crystallizing evaporator, purification system and purification process Download PDFInfo
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- CN106277115B CN106277115B CN201510355385.8A CN201510355385A CN106277115B CN 106277115 B CN106277115 B CN 106277115B CN 201510355385 A CN201510355385 A CN 201510355385A CN 106277115 B CN106277115 B CN 106277115B
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Abstract
The invention discloses a kind of saline sewage crystallizing evaporator, purification system and purification processes, belong to petrochemical industry technical field of sewage.Crystallizing evaporator includes: evaporation and heat-exchange component (D12), gas-liquid separate component (D11) and discharge of materials component (D13)；Wherein, the evaporation and heat-exchange component (D12) includes shell (D10), central tube (D2), heat exchanger tube (D3), steam inlet (D7) and condensation water out (D8)；The central tube (D2) is for conveying saline sewage；The heat exchanger tube (D3) is used for the solvent of concentrating salt-containing sewage, and salt crystallization is precipitated；The internal diameter of the central tube (D2) is greater than the internal diameter of the heat exchanger tube (D3)；Above-mentioned crystallizing evaporator is also applied in saline sewage evaporative crystallization purification system by the present invention, and is optimized to the technological parameter of purification system operation.The purification system and purification process ensure that the clean-up effect of saline sewage on the basis of reducing purification system occupied area, reducing energy consumption.
Description
Technical field
The present invention relates to petrochemical industry technical field of sewage, in particular to a kind of saline sewage evaporative crystallization
Device, purification system and purification process.
Background technique
Petrochemical industry can generate the higher sewage of salt content in process of production.Dirt higher for this kind of salt content
The method that water generally uses evaporative crystallization purifies it.
Currently used evaporative crystallization technique mainly includes calm the anger evaporative crystallization technique and continuous evaporative crystallization technique.Its
In, evaporative crystallization technique of calming the anger are as follows: in evaporation and crystal process, sewage initially enters heat exchanger, then enters steaming through circulating pump
Hair device is evaporated, and the gas-liquid mixture after evaporation enters gas-liquid separator, and isolated secondary steam is laggard through compressor
Enter evaporator as heat source for evaporating, isolated liquid sends evaporator back to after circulating pump and continues to evaporate；Continuously
Evaporation and crystallization system mainly includes the equipment such as multiple-effect evaporation group and circulating pump, includes again evaporator in each effect evaporation group, changes
The equipment such as hot device, crystallization leg.Wherein, evaporator is used to evaporate the solvent of sewage, the concentration of Lai Tigao sewage；Heat exchanger be used to pair
Sewage is heated；Crystallization leg is used to collect the crystal of precipitation.Sewage successively carries out solvent evaporation, sewage by each effect evaporation group
Concentration be continuously improved, after reaching supersaturation, salt crystallizes precipitation from solution.
In the implementation of the present invention, the inventors discovered that in the prior art the prior art has at least the following problems: existing contain
In salt sewage evaporation purging by crystallization technique, occupation area of equipment is big, energy consumption is higher.
Summary of the invention
In order to solve the above technical problems, the present invention provides that a kind of occupied area is small, the lower saline sewage of energy consumption steams
Send out crystallizer, purification system and purification process.
Specifically, including technical solution below:
First aspect present invention provides a kind of saline sewage crystallizing evaporator: the crystallizing evaporator includes:
Salt crystallization is precipitated for evaporating the solvent in the saline sewage in evaporation and heat-exchange component；Gas-liquid separate component,
Gas in steam and liquid separation for evaporating the evaporation and heat-exchange component；And discharge of materials component, it is used for
By after evaporation saline sewage and gained crystal exported from the crystallizing evaporator；
The gas-liquid separate component is connected to the top of the evaporation and heat-exchange component；The discharge of materials component and the steaming
Send out the bottom connection of heat exchanger components；
Wherein,
The evaporation and heat-exchange component includes: shell, central tube, heat exchanger tube, steam inlet and condensation water out；In described
Heart pipe is for conveying saline sewage；The heat exchanger tube is used for the solvent of concentrating salt-containing sewage, and salt crystallization is precipitated；The central tube
And heat exchanger tube is located in the shell portion, the central tube is parallel with the heat exchanger tube, the central tube and the heat exchange
The both ends of pipe respectively with the gas-liquid separate component and the discharge of materials members；The steam inlet is located at the shell
Top, the condensation water out are located at the outer casing underpart；The relationship of the internal diameter of the internal diameter of the central tube and the heat exchanger tube
Are as follows: n0.5d2≤d1≤2n0.5d2, wherein d1For the internal diameter of the central tube, d2For the internal diameter of the heat exchanger tube, n is the heat exchange
The quantity of pipe；
The gas-liquid separate component includes gas-liquid separator, material inlet and steam (vapor) outlet, and the steam (vapor) outlet is located at
Above the gas-liquid separator, the material inlet is located at below the gas-liquid separator；
The discharge of materials component includes hopper and material outlet.
Preferably, the quantity of the central tube is 1, and the quantity of the heat exchanger tube is 50~300.
Preferably, the height of the gas-liquid separator is 150~300mm.
Preferably, the shape of the hopper is taper.
Second aspect of the present invention, which provides, a kind of steams saline sewage using the crystallizing evaporator of first aspect present invention
The purification system of purging by crystallization is sent out, the purification system includes:
Saline sewage intake pipeline, the saline sewage intake pipeline are used to saline sewage being delivered to the evaporative crystallization
Purification system；Head effect crystallizing evaporator, the first effect crystallizing evaporator are the crystallizing evaporator of first aspect present invention, and head effect is steamed
Hair crystallizer material inlet is connected to the saline sewage intake pipeline；End effect crystallizing evaporator, the end effect crystallizing evaporator
For the crystallizing evaporator of first aspect present invention, end effect crystallizing evaporator material inlet and first effect crystallizing evaporator material outlet connect
Logical, end effect crystallizing evaporator steam (vapor) outlet is connected to head effect crystallizing evaporator steam inlet；Heat source intake pipeline, it is described to add
Heat source intake pipeline is connected to end effect crystallizing evaporator steam inlet；And vacuum pump, the vacuum pump and first effect evaporation knot
Brilliant device steam (vapor) outlet connection, for being vacuumized to the evaporative crystallization purification system.
Further, the evaporative crystallization purification system further include: centre effect crystallizing evaporator, the intermediate effect evaporation knot
Brilliant device is located between the first effect crystallizing evaporator and end effect crystallizing evaporator, and the intermediate effect crystallizing evaporator is the present invention the
The crystallizing evaporator of one side, centre effect crystallizing evaporator material inlet are connected to the first effect crystallizing evaporator material outlet,
Centre effect crystallizing evaporator steam (vapor) outlet is connected to the first effect crystallizing evaporator steam inlet；Centre effect crystallizing evaporator material
Outlet is connected to the end effect crystallizing evaporator material inlet, and centre effect crystallizing evaporator steam inlet and end effect evaporation are tied
Brilliant device steam (vapor) outlet connection.
Preferably, the quantity of the intermediate effect evaporator is 1~4.
Further, the evaporative crystallization purification system further include: Rose Box, the Rose Box and end effect crystallizing evaporator
Material outlet connection；Saline slot, the saline slot are connected to the Rose Box；First the first pump intake of water pump and the salt
Sink connection, the first pump outlet are connected to the end effect crystallizing evaporator material inlet.
Further, the evaporative crystallization purification system further include: steam condenser and vacuum tank, the steam condensation
Device and vacuum tank are located on the pipeline that first effect crystallizing evaporator steam (vapor) outlet is connected to vacuum pump, steam condenser inlet and institute
State first effect crystallizing evaporator steam (vapor) outlet connection, steam condensator outlet is connected to vacuum tank entrance, vacuum tank second outlet and
The vacuum pump connection.
Further, the evaporative crystallization purification system further include: water pot, the water pot include clear water zone and contraminated zone,
The clear water zone and first effect crystallizing evaporator condensation water out and intermediate effect crystallizing evaporator condensed water outlet；The dirt
Pool is connected to vacuum tank first outlet.
Further, the evaporative crystallization purification system further include: the first condensed water export pipeline, first condensed water
Export pipeline and end effect crystallizing evaporator condensed water outlet.
Preferably, the first condensed water export pipeline intersects with the saline sewage intake pipeline, in the intersection
It is provided with preheater.
Further, surge tank and feed pump are additionally provided on the saline sewage intake pipeline.
Further, the evaporative crystallization purification system further include: the second condensed water export pipeline, second condensed water
Export pipeline is connected to the contraminated zone of the water pot；And third condensed water export pipeline, the third condensed water export pipeline
It is connected to the clear water zone of the water pot.
Third aspect present invention provides a kind of saline sewage evaporative crystallization purification of system using second aspect of the present invention
Technique.The purification process are as follows:
Initial saline sewage is delivered to first effect crystallizing evaporator, it is dirty to initial saliferous in the first effect crystallizing evaporator
Water is evaporated, and obtains the second saline sewage and third secondary steam；Second saline sewage is delivered to end effect crystallizing evaporator,
Second saline sewage is evaporated in the end effect crystallizing evaporator, obtains third saline sewage, crystal and
Two secondary steams；The second secondary steam is delivered to first effect crystallizing evaporator, the initial saline sewage is heated
Make its evaporation；Heat source is delivered to end effect crystallizing evaporator, carrying out heating to second saline sewage makes its evaporation；Institute
It states first effect crystallizing evaporator and end effect crystallizing evaporator is the crystallizing evaporator of first aspect present invention；
It is vacuumized, is made inside the first effect crystallizing evaporator and end effect crystallizing evaporator in vacuum shape using vacuum pump
State, the end effect crystallizing evaporator internal pressure are greater than the first effect crystallizing evaporator internal pressure；The end effect evaporative crystallization
The temperature of device is greater than the temperature of the first effect crystallizing evaporator.
Preferably, the temperature of the first effect crystallizing evaporator is 45~50 DEG C, and the temperature of the end effect crystallizing evaporator is
70~75 DEG C, the temperature of the heat source is 85~95 DEG C；The first effect crystallizing evaporator internal pressure is 9.5~10KPa,
The end effect crystallizing evaporator internal pressure is 36~36.5KPa.
Further, the purification process further include: second saline sewage is delivered to intermediate effect crystallizing evaporator,
Heating evaporation is carried out using the second secondary steam in the intermediate effect evaporator, gained saline sewage is delivered to the end
Crystallizing evaporator is imitated, gained secondary steam is delivered to first effect crystallizing evaporator；The intermediate effect crystallizing evaporator is the present invention the
The crystallizing evaporator of one side；Inside the first effect crystallizing evaporator, intermediate effect crystallizing evaporator and end effect crystallizing evaporator
Pressure successively increases, and the temperature of the first effect crystallizing evaporator, intermediate effect crystallizing evaporator and end effect crystallizing evaporator is successively
It increases.
Preferably, the quantity of the intermediate effect crystallizing evaporator is 1~4.
Further, the purification process further include: the third saline sewage and crystal for obtaining end effect crystallizing evaporator
It is delivered to Rose Box, the third saline sewage enters saline slot after crystal is filtered, then is transmitted back to end effect by the first water pump and steams
Crystallizer is sent out, is evaporated in the end effect crystallizing evaporator together with the second saline sewage.
Further, the purification process further include: the first condensed water for obtaining first effect crystallizing evaporator and centre
The condensed water that effect crystallizing evaporator obtains is delivered to the clear water zone of water pot；The third that the first effect crystallizing evaporator is obtained is secondary
Steam is delivered to steam condenser, and the third condensed water condensed in the steam condenser is delivered to water after vacuum tank
The contraminated zone of tank.
Further, the purification process further include: the second condensed water obtained using end effect crystallizing evaporator is to initial
Salting liquid is heated.
Further, the purification process further include: convey the third condensed water in the contraminated zone for entering water pot
It is defeated by the condensed water that crystallizing evaporator obtains is imitated with centre into the first condensed water in the clear water zone of water pot to homogeneous conditioning tank
It send to clean water tank.
Saline sewage crystallizing evaporator, purification system and purification process of the invention is not only applicable to petrochemical industry row
The purified treatment of industry saline sewage, additionally it is possible to be related to the field of evaporative crystallization, such as industrial chemicals production for other.
Technical solution provided in an embodiment of the present invention the utility model has the advantages that
1, crystallizing evaporator provided in an embodiment of the present invention is a kind of Novel steam for integrating heat exchange, evaporation and crystallization
Send out crystallizer.When saline sewage enters central tube and flows out from center tube bottom end, understands the principle due to thermal siphon and be inhaled into
In heat exchanger tube, precipitated crystal after a part of solvent is evaporated in heat exchanger tube.The gas-liquid mixture evaporated in heat exchanger tube into
Enter gas-liquid separate component carry out gas-liquid separation, the crystal of the liquid, precipitation that are not evaporated and from central tube flow out and do not inhaled
The sewage for entering heat exchanger tube enters discharge of materials component.The crystallizing evaporator does not need power-equipment, such as compressor, circulating pump
Deng heat exchange, evaporation and the crystallization process to saline sewage can be realized, energy consumption is lower, energy saving, reduce cost.And
The evaporated crystallization device occupied area is small, saves space.
2, above-mentioned crystallizing evaporator is applied in continuous evaporative crystallization system by the embodiment of the present invention, by multiple evaporative crystallizations
Device is cascaded, and purifies to saline sewage, and vacuum pump is arranged in purification system, vacuumizes to purification system, makes every
A crystallizing evaporator is run under vacuum conditions, can reduce the boiling point of saline sewage, makes saline sewage at a lower temperature
It can evaporate, reduce energy consumption.
3, it is additionally provided with the water pot for recycling condensed water in the purification system of the embodiment of the present invention, can effectively solve stone
The oily purified Utilizing question of chemical industry saline sewage reduces sewage discharge, while protecting environment, saves water resource.
In addition, purification system provided in an embodiment of the present invention and purification process can satisfy the requirement of continuous feed, continuous pulp discharge, operation
Steadily.
Detailed description of the invention
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for
For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings other
Attached drawing.
Fig. 1 is the structural schematic diagram of the crystallizing evaporator of the embodiment of the present invention；
Fig. 2 is the operation principle schematic diagram of the crystallizing evaporator of the embodiment of the present invention；
Fig. 3 is the structural schematic diagram of the saline sewage purification system of the embodiment of the present invention；
Fig. 4 is the structural schematic diagram of first effect crystallizing evaporator in the saline sewage purification system of the embodiment of the present invention；
Fig. 5 is the structural schematic diagram of end effect crystallizing evaporator in the saline sewage purification system of the embodiment of the present invention；
Fig. 6 is the process flow chart of the saline sewage purification process of the embodiment of the present invention；
Fig. 7 is process flow when intermediate effect evaporator quantity is 4 in the saline sewage purification process of the embodiment of the present invention
Schematic diagram.
Appended drawing reference respectively indicates in figure:
D1, gas-liquid separator；D2, central tube；D3, heat exchanger tube；D4, hopper；D5, material outlet；D6, steam (vapor) outlet；D7,
Steam inlet；D8, condensation water out；D9, material outlet；D10, shell；D11, gas-liquid separate component；D12, evaporation and heat-exchange portion
Part；D13, discharge of materials component；
A1, saline sewage；A2, the saline sewage for not being inhaled into heat exchanger tube；B1, gas-liquid mixture；B2, the liquid not being evaporated
The crystal of body and precipitation；Steam after b3, gas-liquid separation；Liquid after b4, gas-liquid separation；C1, heat source stream；C2, heat source steam
The cooling obtained condensed water of vapour；
1, surge tank；2, feed pump；3, preheater；
4, first effect crystallizing evaporator；405, first effect crystallizing evaporator material outlet；406, first effect crystallizing evaporator steam goes out
Mouthful；407, first effect crystallizing evaporator steam inlet；408, first effect crystallizing evaporator condenses water out；409, first effect crystallizing evaporator
Material inlet；
5, end effect crystallizing evaporator；505, end effect crystallizing evaporator material outlet；506, end effect crystallizing evaporator steam goes out
Mouthful；507, end effect crystallizing evaporator steam inlet；508, end effect crystallizing evaporator condenses water out；509, end effect crystallizing evaporator
Material inlet；
6, steam condenser；
7, vacuum tank；701, vacuum tank entrance；702, vacuum tank first outlet；703, vacuum tank second outlet；
8, vacuum pump；
9, water pot；901, clear water zone；902, contraminated zone；
10, the second water pump；11, third water pump；12, Rose Box；13, the first water pump；14, saline slot；
15, crystallizing evaporator is imitated in the first centre；16, crystallizing evaporator is imitated in the second centre；
17, crystallizing evaporator is imitated among third；18, crystallizing evaporator is imitated in the 4th centre.
19, saline sewage intake pipeline；20, heat source intake pipeline；
21, the first condensed water export pipeline；22, the second condensed water export pipeline；
23, third condensed water export pipeline；
S1, initial saline sewage；S2, the second saline sewage；S3, third saline sewage；S4, the 4th saline sewage；S5,
Five saline sewages；S6, the 6th saline sewage；S7, the 7th saline sewage；
Q1, heat source；Q2, second secondary steam；Q3, third secondary steam；Q4, the 4th secondary steam；Q5, the five or two
Secondary steam；Q6, the 6th secondary steam；Q7, the 7th secondary steam；
N1, the first condensed water；N2, the second condensed water；N3, third condensed water；N4, the 4th condensed water；N5, the 5th condensation
Water；N6, the 6th condensed water；N7, the 7th condensed water.
Arrow direction in figure indicates the flow direction of gas or liquid.
Specific embodiment
To keep technical solution of the present invention and advantage clearer, below in conjunction with attached drawing to embodiment of the present invention make into
One step it is described in detail.
First aspect present invention provides a kind of saline sewage crystallizing evaporator, the structure of the crystallizing evaporator such as Fig. 1 institute
Show, which includes:
Salt crystallization is precipitated for evaporating the solvent in the saline sewage in evaporation and heat-exchange component D12；
Gas-liquid separate component D11, the gas and liquid in steam for evaporating the evaporation and heat-exchange component D12
Separation；And
Discharge of materials component D13, for after evaporating saline sewage and gained crystal it is defeated from the crystallizing evaporator
Out；
The gas-liquid separate component D11 is connected to the top of the evaporation and heat-exchange component D12；The discharge of materials component
D13 is connected to the bottom of the evaporation and heat-exchange component D12；
Wherein,
The evaporation and heat-exchange component D12 includes: shell D10, central tube D2, heat exchanger tube D3, steam inlet D7 and condensation
Water out D8；
The central tube D2 is for conveying saline sewage；The heat exchanger tube D3 is used for the solvent of concentrating salt-containing sewage, makes salt
Crystallization is precipitated；The central tube D2 and heat exchanger tube D3 is located inside the shell D10, the central tube D2 and the heat exchanger tube
D3 is parallel, the both ends of the central tube D2 and the heat exchanger tube D3 respectively with the gas-liquid separate component D11 and the material
Discharging unit for discharging D13 connection；The steam inlet D7 is located at the top the shell D10, and the condensation water out D8 is located at described outer
The lower part shell D10；
The relationship of the internal diameter of the internal diameter of the central tube and the heat exchanger tube are as follows: n0.5d2≤d1≤2n0.5d2, wherein d1For
The internal diameter of the central tube, d2For the internal diameter of the heat exchanger tube, n is the quantity of the heat exchanger tube；
The gas-liquid separate component D11 includes gas-liquid separator D1, material inlet D9 and steam (vapor) outlet D6, the steam
It exports D6 to be located above the gas-liquid separator D1, the material inlet D9 is located at below the gas-liquid separator D1；
The discharge of materials component D13 includes hopper D4 and material outlet D5.
Referring to fig. 2, the working principle of crystallizing evaporator provided in an embodiment of the present invention is: in the first of crystallizing evaporator operation
Phase, saline sewage a1 enters gas-liquid separate component D11 from material inlet D9, and then enters in central tube D2 and heat exchanger tube D3, heat
Source steam c1 is from the shell D10 that steam inlet D7 enters evaporation and heat-exchange component D12 and transfers heat to central tube D2 and changes
Evaporation generation gas after salting liquid a1 in saline sewage a1 in heat pipe D3, central tube D2 and heat exchanger D3 is heated, but by
Larger in the internal diameter of central tube D2, the amount of the steam generated after heated is less；And heat exchanger tube D3 internal diameter is smaller, generates after heated
Quantity of steam is larger；Since gas density is less than fluid density, density contrast is generated in central tube D2 and heat exchanger tube D3, according to
The principle of " thermal siphon ", the saline sewage a1 in central tube D2 can be inhaled when flowing out from the bottom central tube D2 due to density contrast
Enter in heat exchanger tube D3.Into the saline sewage a1 of heat exchanger tube D3 solvent it is heated after can evaporate, the steam evaporated is by exchanging heat
It is output and then enter gas-liquid separate component D11 at the top of pipe D3, having some vapor to condense in gas-liquid separate component D11, to form gas-liquid mixed
Object b1 is closed, gas-liquid separator D1 of the gas-liquid mixture b1 in gas-liquid separate component D11 carries out gas-liquid separation.Work as evaporative crystallization
After device operation a period of time reaches stable state, since the steam that solvent evaporation generates constantly is exported from heat exchanger tube D3, saliferous
Sewage a1 is not further into heat exchanger tube D3.At this point, saline sewage a1 is flowed from above to below in central tube D2, when from central tube
The bottom D2 flow out when, a part of saline sewage a1 due to " thermal siphon " principle and be inhaled into heat exchanger tube D3, in heat exchanger tube D3
By exchanging with the heat of heat source stream c1, a part of solvent is evaporated, and the steam evaporated at the top of heat exchanger tube D3 by entering
Gas-liquid separate component D11 has some vapor to condense to form gas-liquid mixture b1 in gas-liquid separate component D11, the gas-liquid mixed
Object b1 carries out gas-liquid separation in gas-liquid separate component D11.Liquid b4 after gas-liquid separation is flowed back into central tube D2, gas-liquid point
Gas b3 from after is exported by steam (vapor) outlet D6.Such circular flow, when the salting liquid for being inhaled into heat exchanger tube D3 reaches saturation,
Salt therein will crystallize precipitation.Saline sewage a2 and the heat exchange of heat exchanger tube D3 are flowed out and are not inhaled into from the bottom central tube D2
The crystal of the liquid and precipitation that are not evaporated in pipe D3 enters in the hopper D4 of discharge of materials component D13, defeated by material outlet D5
Out.Heat source stream c1 is condensed into liquid, the condensed water c2 of formation after exchanging with the saline sewage a1 heat in heat exchanger tube D3
It is exported by the condensation water out D8 of evaporation and heat-exchange component D12.
To sum up, crystallizing evaporator provided in an embodiment of the present invention integrates heat exchange, evaporation and crystallization, is not needing to follow
Under the premise of the power-equipments such as ring pump, compressor, heat exchange, evaporation and the knot to salting liquid are realized using " thermal siphon " principle
Brilliant process, is effectively reduced energy consumption, energy saving, reduce cost, at the same also overcome traditional evaporation crystallization equipment heat exchanger and
The problem of evaporator is provided separately reduces the occupied area of crystallizing evaporator, saves space.Moreover, in an evaporative crystallization
In device.Saline sewage can be carried out multiple solvent evaporation, be conducive to that more crystal are precipitated, to reduce saline sewage
Salt content.
In above-mentioned crystallizing evaporator, the quantity of the central tube D2 includes but is not limited to 1, and preferably 1；It is described to change
The quantity of heat pipe D3 preferably 50~300, such as can be 100,150,200 or 250 etc..
In above-mentioned crystallizing evaporator, the internal diameter of the central tube D2 and the relationship of the internal diameter of the heat exchanger tube D3 are excellent
Choosing: n0.5d2≤d1≤2n0.5d2, wherein d1For the internal diameter of the central tube D2, d2For the internal diameter of the heat exchanger tube D3, n is described
The quantity of heat exchanger tube D3.If the internal diameter of heat exchanger tube D3 is larger, i.e., it then will lead to entrance away from smaller with the difference in internal diameters of central tube D2
The solvent of salting liquid in heat exchanger tube D3 cannot largely be evaporated, and keep " thermal siphon " phenomenon unobvious.If heat exchanger tube D3's
Internal diameter is too small, then the saline sewage a1 heat exchanger tube D3 more difficult to get access flowed out from the bottom central tube D2 is influencing the crystallizing evaporator just
Often operation.
In above-mentioned crystallizing evaporator, highly preferred 150~300mm of the gas-liquid separator D1.Gas-liquid separator
The height of D1 is too low, then gas-liquid separation can be made insufficient；And the excessive height of gas-liquid separator 1, then it will increase crystallizing evaporator
Whole volume.
In above-mentioned crystallizing evaporator, the shape of the hopper D4 does not have strict requirements, but conveyed from material
From the aspect of effect, hopper D4's is preferably shaped to taper.
Second aspect of the present invention, which provides, a kind of steams saline sewage using the crystallizing evaporator of first aspect present invention
The purification system of purging by crystallization is sent out, the structural schematic diagram of the purification system is as shown in figure 3, and combine Fig. 4 and Fig. 5, the purification system
System includes:
Saline sewage intake pipeline 19, the saline sewage intake pipeline 19 are used to saline sewage being delivered to the evaporation
Purging by crystallization system；
Head effect crystallizing evaporator 4, the first effect crystallizing evaporator 4 are the crystallizing evaporator of first aspect present invention, head effect
Crystallizing evaporator material inlet 409 is connected to the saline sewage intake pipeline 19；
End effect crystallizing evaporator 5, the end effect crystallizing evaporator 5 are the crystallizing evaporator of first aspect present invention, end effect
Crystallizing evaporator material inlet 509 is connected to head effect crystallizing evaporator material outlet 405, end effect crystallizing evaporator steam (vapor) outlet
506 are connected to head effect crystallizing evaporator steam inlet 407；
Heat source intake pipeline 20, the heat source intake pipeline 20 and end effect crystallizing evaporator steam inlet 507
Connection；And
Vacuum pump 8, the vacuum pump 8 is connected to head effect crystallizing evaporator steam (vapor) outlet 406, for the evaporative crystallization
Purification system vacuumizes.
It is cascaded the crystallizing evaporator of multiple first aspect present invention to form continuous evaporation in above-mentioned purification system
Crystal system, in conjunction with Fig. 4, the working principle of the purification system are as follows:
Initial saline sewage S1 is confessed one's crime by saline sewage intake pipeline 19 imitates crystallizing evaporator material inlet 409 into head
Crystallizing evaporator 4 is imitated, according to the explanation of the working principle of crystallizing evaporator above to the first aspect of the present invention, initial saliferous is dirty
Water S1 is evaporated after entering first effect crystallizing evaporator 4 according to the principle of " thermal siphon ", obtained third secondary steam Q3 (solvent
The steam generated after evaporation is equivalent to the gas-liquid of the output of spontaneous evaporation crystallizer steam (vapor) outlet D6 described in first aspect present invention
Steam b3 after separation, similarly hereinafter) output of You Shouxiao crystallizing evaporator steam (vapor) outlet 406, the second obtained saline sewage S2 is (quite
What the spontaneous evaporation crystallizer material outlet D5 described in first aspect present invention was exported does not enter heat exchanger tube D3 and heat exchanger tube
Unevaporated saline sewage in D3) You Shouxiao crystallizing evaporator material outlet 405 export after entered by end effect crystallizing evaporator material
Mouth 509 enters end effect crystallizing evaporator 5, carries out also according to the working principle of the crystallizing evaporator of first aspect present invention into one
Step evaporation, obtained second secondary steam Q2 is by imitating crystallizing evaporator by head after the output of end effect crystallizing evaporator steam (vapor) outlet 506
The saline sewage that steam inlet 407 enters in first 4 pairs of effect crystallizing evaporator first effect crystallizing evaporator heat exchanger tubes heats.Heating
Heat source Q1 enters end effect crystallizing evaporator 5 by end effect crystallizing evaporator steam inlet 507 by heat source intake pipeline 20, right
Saline sewage in end effect crystallizing evaporator heat exchanger tube is heated.Due to the saliferous concentration of wastewater in end effect crystallizing evaporator 5
Reach supersaturation, salt crystallization therein is precipitated, so that the salt content in saline sewage be made to reduce, achievees the purpose that sewage purification.
In purification system operational process, vacuum pump 8 vacuumizes purification system, transports each effect crystallizing evaporator under vacuum conditions
Row.Since the boiling point of saline sewage under vacuum conditions can reduce, the purification system of the embodiment of the present invention can be lower
At a temperature of run, be on the one hand conducive to the evaporation of saline sewage, on the other hand can reduce the operation energy consumption of purification system.And
And in purification system provided in an embodiment of the present invention, previous effect is evaporated using the secondary steam that latter effect crystallizing evaporator generates
Saline sewage in crystallizer is heated, and heat source is rationally utilized, and further decreases energy consumption, is economized on resources.
In above-mentioned evaporative crystallization purification system, in order to enable more crystal in saline sewage to be precipitated, further
The salt content in sewage is reduced, evaporation knot can be imitated among setting between head effect crystallizing evaporator 4 and end effect crystallizing evaporator 5
Brilliant device.Centre effect crystallizing evaporator is still the crystallizing evaporator that first aspect present invention provides.Centre effect crystallizing evaporator material
Entrance is connected to head effect crystallizing evaporator material outlet 405, centre effect crystallizing evaporator steam (vapor) outlet and first effect crystallizing evaporator
Steam inlet 407 is connected to；Centre effect crystallizing evaporator material outlet is connected to end effect crystallizing evaporator material inlet 509, intermediate
Effect crystallizing evaporator steam inlet is connected to end effect crystallizing evaporator steam (vapor) outlet 506.It confesses one's crime and imitates crystallizing evaporator material outlet
Second saline sewage S2 of 405 outputs enters intermediate effect crystallizing evaporator by centre effect crystallizing evaporator material inlet and is evaporated
Afterwards, then by centre effect crystallizing evaporator material outlet output, and continue to evaporate into end effect crystallizing evaporator 5.Centre effect
The quantity of crystallizing evaporator is preferably 1~4, can be 1,2,3 or 4.When the number of intermediate effect crystallizing evaporator
Connection type and first effect crystallizing evaporator and end effect evaporative crystallization when amount is 2 or more, between each intermediate effect crystallizing evaporator
Connection type between device is identical, i.e., the steam (vapor) outlet of current crystallizing evaporator with and its adjacent upper effect crystallizing evaporator steam
The connection of vapour entrance, the material outlet of current crystallizing evaporator with and its adjacent next effect crystallizing evaporator material inlet connection.
In order to improve the clean-up effect of saline sewage, more crystal be precipitated, above-mentioned evaporative crystallization purification system is also wrapped
Include: Rose Box 12, the Rose Box 12 are connected to end effect crystallizing evaporator material outlet 505；Saline slot 14, the saline slot 14
It is connected to the Rose Box 12；First water pump 13, the first pump intake (not marking in figure) are connected to the saline slot 14, the
One pump outlet (not marking in figure) is connected to the end effect crystallizing evaporator material inlet 509.By end effect crystallizing evaporator
The crystal of third saline sewage S3 and precipitation that material outlet 505 exports enter Rose Box 12 and are filtered, the crystalline substance of the precipitation
Body stays in Rose Box, and third saline sewage S3 enters saline slot 14, is transmitted back to end effect crystallizing evaporator 5 by the first water pump 13
Continue to evaporate.
Above-mentioned evaporative crystallization purification system further include: steam condenser 6 and vacuum tank 7, the steam condenser 6 with
And vacuum tank 7 is located on the pipeline that first effect crystallizing evaporator steam (vapor) outlet 406 is connected to vacuum pump 8, steam condenser inlet (figure
In do not mark) be connected to the first effect crystallizing evaporator steam (vapor) outlet 406, steam condensator outlet (not marked in figure) and vacuum
Tank entrance 701 is connected to, and vacuum tank second outlet 703 is connected to the vacuum pump.It is defeated by head effect crystallizing evaporator steam (vapor) outlet 406
Third steam Q3 out enters vacuum tank 7 after the condensation of steam condenser 6.Not condensed steam is by vacuum tank second outlet
703 outputs.
In order to realize the recycling and reusing of water resource, above-mentioned evaporative crystallization purification system further includes water pot 9.The water pot
9 include clear water zone 901 and contraminated zone 902, and the clear water zone 901 condenses water out 408 and centre with first effect crystallizing evaporator
Imitate crystallizing evaporator condensed water outlet；The contraminated zone 901 is connected to vacuum tank first outlet 702.In steam condenser 6
Middle condense after obtained condensed water enters vacuum tank 7 is exported the contraminated zone 901 for entering water pot 9 by vacuum tank first outlet 702.By
Head effect crystallizing evaporator condensation water out 408 and the condensed water of intermediate effect crystallizing evaporator condensation water out output enter water pot 9
Clear water zone 901.It is solidifying that second be connected to the contraminated zone of the water pot can also be set in above-mentioned evaporative crystallization purification system
Export pipeline 22 is born water, and the third condensed water export pipeline 23 being connected to the clear water zone of the water pot.And it is solidifying second
It bears water and the second water pump 10 is set on export pipeline 22, third water pump 11 is set on third condensed water export pipeline 23.Clear water zone
Water impurity in 901 is less, therefore directly can be delivered to the water bunkerage such as clear water reserviors by third condensed water export pipeline 23
Carry out storage use.And the water in contraminated zone 902 is to condense to obtain after being evaporated by the solvent of initial saline sewage, impurity content phase
To higher, therefore it can be delivered to homogeneous conditioning tank by the second condensed water export pipeline 22 and carry out homogeneous, be that impurity therein contains
Amount reduce after carry out using.
In above-mentioned evaporative crystallization purification system further include: the first condensed water export pipeline 21, first condensed water are defeated
Pipeline 21 and end effect crystallizing evaporator condensed water outlet out.Saliferous in heat source Q1 and end effect crystallizing evaporator 5 is dirty
The condensed water obtained after water heat exchange is exported by the first condensed water export pipeline 21.It is solidifying due to being exported by end effect crystallizing evaporator 5
Temperature still with higher is born water, therefore can use it and initial saline sewage S1 is preheated, realizes the effective of the energy
It utilizes.Therefore, the first condensed water export pipeline 21 can be intersected with saline sewage intake pipeline 19, is arranged in intersection and preheats
Device 3.
It further include the surge tank 1 being arranged on the saline sewage intake pipeline 19 in above-mentioned evaporative crystallization purification system
And feed pump 2.The flow velocity that initial saline sewage S1 enters first effect crystallizing evaporator 4 is adjusted by surge tank 1 and feed pump 2,
Make evaporative crystallization purification system even running.
Third aspect present invention provides a kind of saline sewage evaporative crystallization of purification system using second aspect of the present invention
Purification process.Referring to fig. 4, the purification process are as follows:
Initial saline sewage S1 is delivered to first effect crystallizing evaporator 4, to initially containing in the first effect crystallizing evaporator 4
Salt sewage S1 is evaporated, and obtains the second saline sewage S2 and third secondary steam Q3；Second saline sewage is conveyed into S2 to end
Crystallizing evaporator 5 is imitated, the second saline sewage S2 is evaporated in the end effect crystallizing evaporator 5, third is obtained and contains
Salt sewage S3, crystal and second secondary steam Q2；The second secondary steam Q2 is delivered to first effect crystallizing evaporator 4, it is right
The initial saline sewage S1, which carries out heating, makes its evaporation；The defeated Q1 of heat source is sent to end effect crystallizing evaporator 5, to described
Two saline sewage S2, which carry out heating, makes its evaporation；The first effect crystallizing evaporator 4 and end effect crystallizing evaporator 5 are the present invention first
The crystallizing evaporator of aspect；It is vacuumized, is made inside the first effect crystallizing evaporator 4 and end effect crystallizing evaporator 5 using vacuum pump 8
In vacuum state, 5 internal pressure of end effect crystallizing evaporator is greater than first effect 4 internal pressure of crystallizing evaporator；It is described
The temperature 5 of end effect crystallizing evaporator is greater than the temperature of the first effect crystallizing evaporator 4.
Evaporative crystallization purification process provided in an embodiment of the present invention is a kind of countercurrent evaporation technique, i.e., the flow direction of steam and contains
The flow direction of salt sewage is opposite.The secondary steam that latter effect crystallizing evaporator generates is to the saline sewage in previous effect crystallizing evaporator
It is heated, can effectively utilize the energy.And in above-mentioned purification process, head effect crystallizing evaporator 4 and end effect evaporative crystallization
Vacuum state is in inside device 5, the boiling point of saline sewage reduces under vacuum conditions, is on the one hand conducive to the steaming of saline sewage
Hair, on the other hand can reduce the operation energy consumption of purification system.
In above-mentioned evaporative crystallization purification process, the temperature of head effect crystallizing evaporator 4 is preferably 45~50 DEG C, and end effect is steamed
The temperature for sending out crystallizer 5 is preferably 70~75 DEG C, and the temperature of heat source is preferably 85~95 DEG C；Inside head effect crystallizing evaporator
Pressure is preferably 9.5~10KPa, and end effect crystallizing evaporator internal pressure is preferably 36~36.5KPa.Wherein, heat source can
To sufficiently recycle the low-temperature heat quantity of refinery, to bring direct economic benefit to enterprise using the low-temperature heat quantity of refinery.
In above-mentioned evaporative crystallization purification process, evaporated when being imitated in the purification system of second aspect of the present invention including centre
When crystallizer, then the second saline sewage S2 is delivered to intermediate effect crystallizing evaporator, the benefit in the intermediate effect evaporator
Heating evaporation is carried out with the second secondary steam Q2 that end effect crystallizing evaporator 5 exports, gained saline sewage is delivered to the end effect
Crystallizing evaporator 5, gained secondary steam are delivered to first effect crystallizing evaporator 4；At this point, the first effect crystallizing evaporator 4, intermediate effect
Crystallizing evaporator and 5 internal pressure of end effect crystallizing evaporator successively increase, and temperature also successively increases.
In order to improve the clean-up effect of saline sewage, more crystal be precipitated, above-mentioned evaporative crystallization purification process is also wrapped
It includes: third saline sewage S3 and crystal that end effect crystallizing evaporator 5 obtains is delivered to Rose Box 12, it is described after crystal is filtered
Third saline sewage S3 enters saline slot 14, then is transmitted back to end effect crystallizing evaporator 5 by the first water pump 13, with the second saline sewage
S2 is evaporated in end effect crystallizing evaporator 5 together.
In order to realize the recycling and reusing of water resource, above-mentioned evaporative crystallization purification process further include: head is imitated evaporation knot
The condensed water that the first condensed water N1 and intermediate effect crystallizing evaporator that brilliant device 4 obtains are obtained is delivered to the clear water zone of water pot 9
901；The third secondary steam Q3 that the first effect crystallizing evaporator obtains is delivered to steam condenser 6, the third condensed
The contraminated zone 902 of water pot 9 is delivered to after condensed water N3 after vacuum tank 7.
In above-mentioned evaporative crystallization purification process, the second condensed water that can also be obtained using end effect crystallizing evaporator 5
N2 heats initial salt solution S1, to realize making full use of for the energy.
It, can also be by the third condensed water in the contraminated zone 902 for entering water pot 9 in above-mentioned evaporative crystallization purification process
N3 is delivered to homogeneous conditioning tank, and the first condensed water N1 in the clear water zone 901 for entering water pot 9 is obtained with intermediate effect crystallizing evaporator
To condensed water be delivered to clear water reserviors, realize the recycling to water resource.
In following embodiment, by taking centre effect evaporator quantity is 4 as an example, i.e., entire evaporative crystallization purification system shares 6 effects
For crystallizing evaporator, saline sewage evaporative crystallization purification process of the invention is described in further detail
Embodiment 1
In the saline sewage evaporative crystallization purification process of the present embodiment, the quantity of central tube D2 is in crystallizing evaporator used
The quantity of 1, heat exchanger tube D3 are 200, and the relationship of the internal diameter d1 of the internal diameter d2 and central tube D2 of heat exchanger tube D3 are d2=14d1, gas-liquid
The height of separator D1 is 200mm.
In the present embodiment, heat source Q1 used is 90 DEG C of the low-temperature water heating from refinery, initial saline sewage S1's
Temperature is 25 DEG C.
In conjunction with Fig. 7, the saline sewage evaporative crystallization purification process of the present embodiment is；
Initial saline sewage S1 initially enters surge tank 1, then conveys after flow is adjusted to 90000kg/h by feed pump 2
To preheater 3, the second condensed water N2 for being 76 DEG C with the temperature from end effect crystallizing evaporator 5 in preheater 3 exchanges heat
Temperature reaches 48 DEG C afterwards, then confesses one's crime and imitates crystallizing evaporator material inlet 409 and enter first effect crystallizing evaporator 4, and comes from first
After the 7th secondary steam Q7 that the temperature of centre effect crystallizing evaporator 15 is 56 DEG C carries out heat exchange evaporation, the secondary steaming of obtained third
Vapour Q3 obtains third condensed water N3, third condensed water N3 warp after steam condenser 6 (thermic load 7.467MKcal/h) is cooling
The contraminated zone 902 that vacuum tank 7 enters water pot 9 is crossed, homogeneous is then delivered to the flow of 12896kg/h by the second water pump 10 and is adjusted
Pond carries out homogeneous.Effect evaporation among first is entered by the second saline sewage S2 that first effect crystallizing evaporator material outlet 405 exports
The 6th secondary steam Q6 for being 60 DEG C with the temperature of the effect crystallizing evaporator 16 among second after crystallizer 15 carries out heat exchange steaming
Hair, the 4th saline sewage S4 of gained enter effect crystallizing evaporator 16 and the effect crystallizing evaporator 17 among third among second
Temperature is that 60 DEG C of the 5th secondary steam Q5 carries out heat exchange evaporation, and the 5th obtained saline sewage S5 enters effect evaporation among third
Crystallizer 17, the 4th secondary steam Q4 that the temperature with the effect crystallizing evaporator 18 among the 4th is 70 DEG C carry out heat exchange steaming
Hair, the 6th saline sewage S6 of gained enter the 4th crystallizing evaporator 18, are 85 DEG C with the temperature from end effect crystallizing evaporator 5
Second secondary steam Q2 carries out heat exchange evaporation, and the 7th obtained saline sewage S7 enters end effect crystallizing evaporator 5 and comes from refinery
Low-temperature water heating at a temperature of 90 °C (i.e. heat source Q1) carry out heat exchange evaporation after, concentration reach supersaturation, salt therein
Crystallization is precipitated, and the crystal and third saline sewage S3 of precipitation enter Rose Box 12 together, and crystal stays in Rose Box 12, and third contains
Salt sewage S3 enters saline slot 14, and the first water pump 13 is defeated with the flow of 6750kg/h by the third saline sewage S3 in saline slot 14
It sends end effect crystallizing evaporator 5 back to and continues heat exchange evaporation.Heat source Q1 is dirty with the 7th saliferous in end effect crystallizing evaporator 5
After water S7 heat exchange, it is defeated by the first condensed water feed-line 21 to obtain the second condensed water N2, the second condensed water N2 that temperature is 76 DEG C
It send to preheater 3 and initial saline sewage S1 is preheated.The first condensed water N1 for being obtained after 7th secondary steam Q7 heat exchange, the
Six secondary steam Q6 heat exchange after obtain the 4th condensed water N4, the 5th secondary steam Q5 heat exchange after obtain the 5th condensed water N5,
The 6th condensed water N6 obtained after 4th secondary steam Q4 heat exchange and the 7th condensed water obtained after second secondary steam Q2 heat exchange
N7 enters the clear water zone 901 of water pot 9, is then delivered to clear water reserviors by third water pump 11 with the flow of 70354kg/h and is recycled
It utilizes.
In above-mentioned evaporation and crystal process, vacuum pump 8 vacuumizes evaporative crystallization purification system, head effect crystallizing evaporator
4, effect crystallizing evaporator 16, third centre are imitated in crystallizing evaporator the 17, the 4th among the first centre effect crystallizing evaporator 15, second
Between imitate the pressure of crystallizing evaporator 18 and end effect crystallizing evaporator 5 and be followed successively by 9.8kPa, 16.1kPa, 20.2kPa,
24.3kPa, 28.6kPa, 36.1kPa, temperature are followed successively by 46 DEG C, and 56 DEG C, 60 DEG C, 65 DEG C, 68 DEG C, 74 DEG C, thermic load is successively are as follows:
7.151MKcal/h、7.878MKcal/h、8.088MKcal/h、8.244MKcal/h、8.331MKcal/h、8.425MKcal/
h。
After the above evaporative crystallization purification process, in the clear water zone 901 of water pot 9 come confess one's crime imitate crystallizing evaporator 4,
Crystallizing evaporator 17 and the 4th is imitated in effect crystallizing evaporator 16, third centre among effect crystallizing evaporator 15, second among first
The property of the condensed water of centre effect crystallizing evaporator 18 is detected according to GB1576-2008, and each with initial saline sewage
Item property compares, and acquired results are as shown in table 1.
1 steam condensate property list of table
| Project | Initial saline sewage | Steam condensate |
| pH | 6-9 | 6.5-8.5 |
| SS(mg/L) | ≤50 | ≤10 |
| CODcr(mg/L) | ≤200 | ≤30 |
| BOD5(mg/L) | ≤12 | ≤5 |
| Petroleum-type (mg/L) | ≤10 | ≤5 |
| Volatile Phenols (mg/L) | ≤0.1 | ≤0.01 |
| NH3-N(mg/L) | ≤12 | ≤3 |
| TDS(mg/L) | ≤5000 | ≤800 |
| Cl-(mg/L) | ≤6500 | ≤200 |
To sum up, the embodiment of the present invention provides firstly a kind of novel evaporation knot for integrating heat exchange, evaporation and crystallization
Brilliant device, low energy consumption for the crystallizing evaporator, occupied area is small.The crystallizing evaporator is applied to continuous evaporation knot by the embodiment of the present invention
In crystallographic system system, multiple crystallizing evaporators are cascaded, saline sewage is purified, vacuum is set in purification system
Pump, vacuumizes purification system, makes purification system at a lower temperature and can be realized as the purification to saline sewage, the present invention
Embodiment also optimizes the technological parameter of above-mentioned saline sewage purification system operation, ensure that on the basis of reducing energy consumption
The clean-up effect of saline sewage.Purification system and purification process provided in an embodiment of the present invention can satisfy continuous feed, continuous
The requirement of discharge, runs smoothly, and can effectively solve the purified Utilizing question of petrochemical industry saline sewage, reduces sewage
Discharge.
The above is merely for convenience of it will be understood by those skilled in the art that technical solution of the present invention, not to limit
The present invention.All within the spirits and principles of the present invention, any modification, equivalent replacement, improvement and so on should be included in this
Within the protection scope of invention.
Claims (16)
1. a kind of saline sewage crystallizing evaporator, which is characterized in that the crystallizing evaporator includes:
Salt crystallization is precipitated for evaporating the solvent in the saline sewage in evaporation and heat-exchange component (D12)；
Gas-liquid separate component (D11), the gas and liquid in steam for obtaining the evaporation and heat-exchange component (D12) evaporation
Separation；And
Discharge of materials component (D13), for exporting the saline sewage after evaporating and gained crystal from the crystallizing evaporator；
The gas-liquid separate component (D11) is connected to the top of the evaporation and heat-exchange component (D12)；The discharge of materials component
(D13) it is connected to the bottom of the evaporation and heat-exchange component (D12)；
Wherein,
The evaporation and heat-exchange component (D12) include: shell (D10), central tube (D2), heat exchanger tube (D3), steam inlet (D7) with
And condensation water out (D8)；
The central tube (D2) is for conveying saline sewage；The heat exchanger tube (D3) is used for the solvent of concentrating salt-containing sewage, makes salt
Crystallization is precipitated；The central tube (D2) and heat exchanger tube (D3) are located at the shell (D10) inside, the central tube (D2) and institute
State heat exchanger tube (D3) in parallel, the both ends of the central tube (D2) and the heat exchanger tube (D3) respectively with the gas-liquid separate component
(D11) it is connected to the discharge of materials component (D13)；The steam inlet (D7) is located at the top the shell (D10), described solidifying
It bears water outlet (D8) and is located at the lower part the shell (D10)；
The relationship of the internal diameter of the internal diameter and heat exchanger tube (D3) of the central tube (D2) are as follows: n0.5d2≤d1≤2n0.5d2, wherein
d1For the internal diameter of the central tube (D2), d2For the internal diameter of the heat exchanger tube (D3), n is the quantity of the heat exchanger tube (D3)；
The gas-liquid separate component (D11) includes gas-liquid separator (D1), material inlet (D9) and steam (vapor) outlet (D6), described
Steam (vapor) outlet (D6) is located above the gas-liquid separator (D1), and the material inlet (D9) is located at the gas-liquid separator (D1)
Lower section；
The discharge of materials component (D13) includes hopper (D4) and material outlet (D5).
2. crystallizing evaporator according to claim 1, which is characterized in that the quantity of the central tube (D2) is 1, described
The quantity of heat exchanger tube (D3) is 50~300.
3. crystallizing evaporator according to claim 1, which is characterized in that the height of the gas-liquid separator (D1) is 150
~300mm.
4. a kind of saline sewage evaporative crystallization purification system, which is characterized in that the purification system includes:
Saline sewage intake pipeline (19), the saline sewage intake pipeline (19) are used to saline sewage being delivered to the evaporation
Purging by crystallization system；
Head effect crystallizing evaporator (4), first effect crystallizing evaporator (4) are crystallizing evaporator described in claim 1, and head effect is steamed
Hair crystallizer material inlet (409) is connected to the saline sewage intake pipeline (19)；
End effect crystallizing evaporator (5), the end effect crystallizing evaporator (5) are crystallizing evaporator described in claim 1, and end effect is steamed
Hair crystallizer material inlet (509) is connected to head effect crystallizing evaporator material outlet (405), end effect crystallizing evaporator steam (vapor) outlet
(506) it is connected to head effect crystallizing evaporator steam inlet (407)；
Heat source intake pipeline (20), the heat source intake pipeline (20) and end effect crystallizing evaporator steam inlet
(507) it is connected to；And
Vacuum pump (8), the vacuum pump (8) are connected to head effect crystallizing evaporator steam (vapor) outlet (406), for tying to the evaporation
Brilliant purification system vacuumizes.
5. evaporative crystallization purification system according to claim 4, which is characterized in that the evaporative crystallization purification system is also wrapped
It includes:
Centre effect crystallizing evaporator, the intermediate effect crystallizing evaporator are located at first effect crystallizing evaporator (4) and end effect evaporation
Between crystallizer (5), the intermediate effect crystallizing evaporator is crystallizing evaporator described in claim 1, centre effect evaporative crystallization
Device material inlet is connected to first effect crystallizing evaporator material outlet (405), centre effect crystallizing evaporator steam (vapor) outlet and institute
State first effect crystallizing evaporator steam inlet (407) connection；Centre effect crystallizing evaporator material outlet and the end effect evaporative crystallization
Device material inlet (509) connection, centre effect crystallizing evaporator steam inlet and the end effect crystallizing evaporator steam (vapor) outlet (506)
Connection.
6. evaporative crystallization purification system according to claim 5, which is characterized in that the quantity of effect evaporator is among described
1~4.
7. evaporative crystallization purification system according to claim 4, which is characterized in that the evaporative crystallization purification system is also wrapped
It includes:
Rose Box (12), the Rose Box (12) are connected to end effect crystallizing evaporator material outlet (505)；
Saline slot (14), the saline slot (14) are connected to the Rose Box (12)；
First water pump (13), the first pump intake are connected to the saline slot (14), the first pump outlet and the end effect
Crystallizing evaporator material inlet (509) connection.
8. evaporative crystallization purification system according to claim 7, which is characterized in that the evaporative crystallization purification system is also wrapped
It includes:
Steam condenser (6) and vacuum tank (7), the steam condenser (6) and vacuum tank (7) are located at first effect evaporative crystallization
On the pipeline that device steam (vapor) outlet (406) is connected to vacuum pump (8), steam condenser inlet and the first effect crystallizing evaporator steam
Export (406) connection, steam condensator outlet be connected to vacuum tank entrance (701), vacuum tank second outlet (703) with it is described very
Sky pump connection.
9. evaporative crystallization purification system according to claim 8, which is characterized in that the evaporative crystallization purification system is also wrapped
It includes:
Water pot (9), the water pot (9) include clear water zone (901) and contraminated zone (902), and the clear water zone (901) and first effect are evaporated
Crystallizer condenses water out (408) and intermediate effect crystallizing evaporator condensed water outlet；The contraminated zone (901) and vacuum
Tank first outlet (702) connection.
10. a kind of saline sewage evaporative crystallization purification process using purification system as claimed in claim 4, which is characterized in that
The purification process are as follows:
Initial saline sewage (S1) is delivered to first effect crystallizing evaporator (4), to initial in first effect crystallizing evaporator (4)
Saline sewage (S1) is evaporated, and obtains the second saline sewage (S2) and third secondary steam (Q3)；
Second saline sewage (S2) is delivered to end effect crystallizing evaporator (5), to described in the end effect crystallizing evaporator (5)
Second saline sewage (S2) is evaporated, and obtains third saline sewage (S3), crystal and second secondary steam (Q2)；It will be described
Second secondary steam (Q2) is delivered to first effect crystallizing evaporator (4), and carrying out heating to the initial saline sewage (S1) makes its steaming
Hair；
Heat source (Q1) is delivered to end effect crystallizing evaporator (5), carrying out heating to second saline sewage (S2) makes it
Evaporation；
First effect crystallizing evaporator (4) and end effect crystallizing evaporator (5) are crystallizing evaporator described in claim 1；
It is vacuumized, is made inside first effect crystallizing evaporator (4) and end effect crystallizing evaporator (5) in true using vacuum pump (8)
Dummy status, end effect crystallizing evaporator (5) internal pressure are greater than described first effect crystallizing evaporator (4) internal pressure；The end
The temperature for imitating crystallizing evaporator (5) is greater than the temperature of first effect crystallizing evaporator (4).
11. purification process according to claim 10, which is characterized in that the temperature of first effect crystallizing evaporator (4) is
45~50 DEG C, the temperature of the end effect crystallizing evaporator (5) is 70~75 DEG C, and the temperature of the heat source (Q1) is 85~95
℃；First effect crystallizing evaporator (4) internal pressure is 9.5~10KPa, and end effect crystallizing evaporator (5) internal pressure is
36~36.5KPa.
12. purification process according to claim 10, which is characterized in that the purification process further include:
Second saline sewage (S2) is delivered to intermediate effect crystallizing evaporator, using described in the intermediate effect evaporator
Second secondary steam (Q2) carries out heating evaporation, and gained saline sewage is delivered to the end effect crystallizing evaporator (5), and gained is secondary
Steam is delivered to first effect crystallizing evaporator (4)；
The intermediate effect crystallizing evaporator is crystallizing evaporator described in claim 1；
First effect crystallizing evaporator (4), intermediate effect crystallizing evaporator and end effect crystallizing evaporator (5) internal pressure successively rise
The temperature of height, first effect crystallizing evaporator (4), intermediate effect crystallizing evaporator and end effect crystallizing evaporator (5) successively increases.
13. purification process according to claim 12, which is characterized in that the quantity of the intermediate effect crystallizing evaporator is 1
~4.
14. purification process according to claim 10, which is characterized in that the purification process further include:
Third saline sewage (S3) and crystal that end effect crystallizing evaporator (5) obtains are delivered to Rose Box (12), by crystal mistake
The third saline sewage (S3) enters saline slot (14) after filter, then is transmitted back to end effect crystallizing evaporator by the first water pump (13)
(5), it is evaporated in the end effect crystallizing evaporator (5) together with the second saline sewage (S2).
15. purification process according to claim 12, which is characterized in that the purification process further include: by head effect evaporation
The condensed water that the first condensed water (N1) and intermediate effect crystallizing evaporator that crystallizer (4) obtains obtain is delivered to water pot (9)
Clear water zone (901)；The third secondary steam (Q3) that first effect crystallizing evaporator (4) obtains is delivered to steam condenser (6),
The third condensed water (N3) that condensation obtains in the steam condenser (6) is delivered to the sewage of water pot (9) after vacuum tank (7)
Area (902).
16. purification process according to claim 10, which is characterized in that the purification process further include:
The second condensed water (N2) obtained using end effect crystallizing evaporator (5) heats initial salt solution (S1).
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| CN113526600B (en) * | 2021-06-17 | 2022-07-26 | 中国恩菲工程技术有限公司 | Desalting and deoxidizing equipment and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN201350354Y (en) * | 2009-01-13 | 2009-11-25 | 姜新明 | Evaporated crystallizer |
| CN203653280U (en) * | 2013-11-21 | 2014-06-18 | 云南黄金矿业集团股份有限公司 | Evaporation crystallization equipment for processing high-salinity wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN201350354Y (en) * | 2009-01-13 | 2009-11-25 | 姜新明 | Evaporated crystallizer |
| CN203653280U (en) * | 2013-11-21 | 2014-06-18 | 云南黄金矿业集团股份有限公司 | Evaporation crystallization equipment for processing high-salinity wastewater |
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