CN109836005A - The processing unit and technique of the high-salt wastewater containing silica in titanium dioxide silicic acid depositing technology - Google Patents
The processing unit and technique of the high-salt wastewater containing silica in titanium dioxide silicic acid depositing technology Download PDFInfo
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Abstract
The present invention provides the processing units and technique of the high-salt wastewater containing silica in a kind of titanium dioxide silicic acid depositing technology.The processing unit includes pretreatment unit, pre-concentration unit, two-effect evaporation unit, MVR evaporative crystallization unit and drying unit, and each unit, which is sequentially connected, to be connect；Pretreatment unit includes subsider；Pre-concentration unit includes that evaporation is cold；Two-effect evaporation unit includes an effect separator, an effect heater, two effect separators, two effect heaters and filter press；MVR evaporative crystallization unit includes MVR heater, MVR separator, MVR compressor, MVR thickener and MVR centrifuge；Drying unit includes drying machine.The condensed water that the technique generates is taken out as industrial water reuse, the precipitation of silica object of generation as hydrated SiO 2 product, and the anhydrous sodium sulfate of generation can be used as chemical products take-away, generates in the process without wastes such as waste water, solid wastes；The zero-emission for realizing waste water, makes classical acid depositing technology be transformed into cleaning procedure.
Description
Technical field
The invention belongs to sewage treatment fields, and in particular to the hydrated SiO 2s product acid precipitation method such as white carbon black and silica gel
The processing unit and technique of the high-salt wastewater containing silica generated in production process.
Background technique
The hydrated SiO 2s product such as white carbon black and silica gel is that white powder X-ray amorphous silicic acid and silicate produce
The general name of product, main component are silica.
Currently, the hydrated SiO 2s product processes such as white carbon black and silica gel are mainly vapor phase method and precipitating both at home and abroad
Method.And the precipitation method are domestic mainly uses sulfuric acid precipitation method, domestic existing white carbon black device is using sodium metasilicate acidization (also known as precipitating
Method) white carbon black is produced, it is reacted using sodium metasilicate with sulfuric acid, generates silica and sodium sulphate, then filtered and with washing
Water repeatedly cleans repeatedly, after sodium sulphate is fallen in removing, surplus material liquefied, dry after obtain product.Filtering, cleaning process difference
It has filtered wastewater (reaction mother liquor) and washes generates, thus white carbon black device technique waste water generates.
Since the raw material cleanliness that white carbon black production uses is high, and production process is entirely inorganic reaction, and no side reaction produces
It is raw, only generate silica and sodium sulphate in production process, therefore technique waste water water quality is preferable, COD generally in 50mg/L hereinafter,
Its major pollutants is total salt quantity (sodium sulphate)；The technique waste water main indicator is as shown in table 1 below.
Table 1
From in 1 data of table it can be seen that silicone content height ranks first in the waste water except sulfuric acid sodium.
The processing of the waste water is mostly handled in such a way that medicament is except silicon+film filtering+evaporation at present, but in operational process
In that there are medicament use costs is high, generates the problems such as big solid waste amount, film surface and evaporating heat exchanger and fouling of waste water face, this
A little problems increase equipment investment and operating cost and then hinder the progress of the water process with high salt containing silica.
Summary of the invention
Based on problems of the prior art, the purpose of the present invention is to provide a kind of SiO2Contain two in sour depositing technology
The processing unit of silica high-salt wastewater；The object of the invention is also to provide a kind of SiO2Contain silica in sour depositing technology
The treatment process of high-salt wastewater；Traditional handicraft is able to solve using the processing unit and its technique to be hydrated white carbon black and silica gel etc.
Solid waste yield in the treatment process of high-salt wastewater containing silica generated in silica product sulfuric acid precipitation method production process
Greatly, it the problem of the bottleneck of operating cost height, equipment scaling, really realizes the zero-emission of the high-salt wastewater containing silica, makes to be hydrated
The sulfuric acid precipitation method process changeover of silica is at process for cleanly preparing.
The purpose of the present invention is achieved by the following technical programs:
On the one hand, the present invention provides a kind of SiO2The processing unit of the high-salt wastewater containing silica in sour depositing technology, should
Processing unit includes pretreatment unit, pre-concentration unit, two-effect evaporation unit, MVR evaporative crystallization unit and drying unit, each list
Member, which is sequentially connected, to be connect；
The pretreatment unit includes subsider, for the silica in initial gross separation recycling waste water；
The pre-concentration unit includes evaporating cold, the preliminary pre-concentration of part evaporation realization of the moisture for waste water；
The two-effect evaporation unit includes an effect separator, an effect heater, two effect separators, two effect heaters and filters pressing
Machine；
The one effect heater is mutually recycled with the effect separator and is connected to, and is provided with and the external world in the effect heater
The first heat exchange pipeline that heat source is connected, first heat exchange pipeline are provided with inlet and outlet；The one effect separator is provided with the
One gas vent, the first liquid inlet and the first liquid outlet；The evaporation is cold to be connected with first liquid inlet；
The two effect heater is mutually recycled with the two effects separator and is connected to, and is provided with and the external world in the two effects heater
The second heat exchange pipeline that heat source is connected, second heat exchange pipeline are provided with inlet and outlet；First gas outlet with it is described
The import of second heat exchange pipeline is connected；The two effects separator is provided with second gas outlet, second liquid entrance and second
Liquid outlet；The second liquid outlet is connected with the filter press；First liquid outlet enters with the second liquid
Mouth is connected；Cold be connected is evaporated with described in the second gas outlet；
The MVR evaporative crystallization unit include MVR heater, MVR separator, MVR compressor, MVR thickener and MVR from
Scheming；
The MVR separator is mutually recycled with the MVR heater and is connected to, and is provided in the MVR heater and external world's heat
The third heat exchange pipeline that source is connected, the third heat exchange pipeline are provided with inlet and outlet；The MVR separator is provided with third gas
Body outlet, third liquid inlet and third liquid outlet；The third gas outlet, the MVR compressor and the third are changed
The import of heat pipeline is connected；The filter press is connected with the third liquid inlet of the MVR separator；The third liquid
Outlet is connected with the MVR thickener；The MVR thickener is connected with the MVR centrifuge；
The drying unit includes drying machine；The MVR centrifuge is connected with the drying machine.
In above-mentioned processing unit, it is preferable that the inlet and outlet of the first heat exchange pipeline of the effect heater are for being connected to
The cyclic ammonia water stream of extraneous coking workshop section.
In above-mentioned processing unit, it is preferable that the pre-concentration unit further includes the first surge tank；First surge tank
Reuse is produced for collecting and storing the cold condensed water of the evaporation.
In above-mentioned processing unit, it is preferable that first surge tank is provided with the first vacuum pump.
In above-mentioned processing unit, it is preferable that the MVR evaporative crystallization unit further includes the second surge tank；Described second
Surge tank is used to collect and store the condensed water production reuse of the outlet of the third heat exchange pipeline.
In above-mentioned processing unit, it is preferable that second surge tank is provided with the second vacuum pump.
In above-mentioned processing unit, it is preferable that set on the cold pipeline being connected with first liquid inlet of evaporation
It is equipped with the first feed pump.
In above-mentioned processing unit, it is preferable that an effect heater mutually recycles the pipe being connected to the effect separator
Road is provided with an effect forced circulation pump.
In above-mentioned processing unit, it is preferable that the two effect heater mutually recycles the pipe being connected to the two effects separator
Road is provided with two effect forced circulation pumps.
In above-mentioned processing unit, it is preferable that the MVR separator mutually recycles the pipeline being connected to the MVR heater
On be provided with MVR forced circulation pump.
In above-mentioned processing unit, it is preferable that the evaporation is cold including scuttlebutt and to be arranged in scuttlebutt periphery
Circulating Pump System；
It is provided with blower, dehydrator is successively vertically provided with along the blower at the top of the scuttlebutt, is water-spray system, cold
But coil pipe and collecting-tank；
The Circulating Pump System includes two water circulating pumps in parallel, and the both ends of the water circulating pump are connected in turn out
Mouth valve and inlet valve, the outlet valve are connected with the dehydrator；The inlet valve is connected with the collecting-tank；
The entrance of the cooling coil is connected with second gas outlet；The outlet of the cooling coil and described the
One surge tank is connected.
In above-mentioned processing unit, it is preferable that the drying machine includes bed body, drying under drying machine upper bed body, drying machine
Machine bellows, drying machine visor, dry elevator and finished product bin；
The MVR centrifuge is connected with the drying machine upper bed body；The outlet of bed body is done with described under the drying machine
Dry elevator is connected；The dry elevator is connected with the finished product bin；The drying machine visor setting is described dry
The bottom of bed body under the drying machine is arranged in the lateral wall of bed body under dry machine, the drying machine bellows；
Preferably, feed auger is additionally provided on the pipeline that the MVR centrifuge is connected with the drying machine upper bed body
Conveyer.
On the other hand, the present invention also provides a kind of SiO2The processing work of the high-salt wastewater containing silica in sour depositing technology
Skill is carried out using above-mentioned processing unit, comprising the following steps:
Step 1, bin cure acid precipitation method hydrated SiO 2 in future produce the high-salt wastewater containing silica and hydrogen-oxygen of workshop section
Changing sodium mixing to adjust pH value of waste water is alkalinity, and carries out sedimentation separation, obtains sediment and supernatant effluent；
Supernatant effluent is sent to evaporating to be used as in cold and evaporates the recirculated cooling water of cold cooling steam, in cooling by step 2
During steam, supernatant effluent has also carried out part and has evaporated, and realizes preliminary pre-concentration；
Step 3, the waste water by preliminary pre-concentration enter in an effect separator, are added by circulation vacuum pump via an effect
Hot device exchanges heat, and the heat source of the first heat exchanger channels in an effect heater is from the cyclic ammonia water of coking workshop section；It is preliminary pre- dense
The waste water of contracting is flashed in Yu Yixiao separator after heat exchange heating；
Step 4, the waste liquid after an effect separator flash concentration enter in two effect separators, force to follow by two effects
Ring pump is exchanged heat again via two effect heaters, and the heat source of the second heat exchanger channels in two effect heaters is from an effect separator
Steam after flash distillation；Waste water is flashed in Yu Erxiao separator after heat exchange heating, and an effect flash-off steam is in two effect heating
Device carries out condensation and is recycled；
Step 5, the waste water after two effect separator flash concentrations enter filtering in filter press and obtain filter cake and filtrate；
Steam after two effect separator flash distillations enters the cold unit of evaporation and carries out condensing recovery utilization；
Step 6, filtrate enter in MVR separator, are exchanged heat by MVR forced circulation pump via MVR heater, MVR
Steaming of the heat source of third heat exchanger channels in heater from the steam that MVR separator flashes after the heating of MVR compressor compresses
Vapour；Filtrate is flashed in MVR separator after heat exchange heating, and flash-off steam is condensed in MVR heater and returned again
It receives and utilizes；
Step 7, the sodium sulfate crystal being precipitated after MVR separator flash concentration successively pass through MVR thickener, MVR from
Solid sodium sulfate is obtained after scheming and drying machine.
In above-mentioned treatment process, it is preferable that in step 1, it is 9-14 that sodium hydroxide, which is added, and adjusts the pH value of waste water,
Preferable ph is 9-10.The pH value can prevent silica fouling in evaporation process；Sodium hydroxide is added simultaneously not only to have
There is the function of adjusting pH, the solubility of soluble silica can also be improved.
In above-mentioned treatment process, it is preferable that in step 2, the evaporating temperature of preliminary pre-concentration is 40-80 DEG C；Negative pressure
For -93.94kPa~-53.91kPa.It can make fouling factor silica in evaporation process using this evaporating temperature and pressure
It is precipitated with floccule or particulate form, the floccule or particulate matter can be flowed with solution, without in evaporator surface shape
At hard, fine and close layer of scale, heat exchange efficiency is caused to reduce, to eliminate high-salt wastewater containing silica in evaporation process
The fouling factor, whole process do not need another adding medicine except silica, had both saved water treatment agent cost, and avoided solid waste
It generates.
In above-mentioned treatment process, it is preferable that in step 3, the temperature of the cyclic ammonia water is 70-80 DEG C, preliminary pre-
Temperature of the waste water of concentration after heat exchange heating is 60-65 DEG C；Vapor (steam) temperature after flash distillation is 55-60 DEG C；One effect point
It is -83.94kPa~-53.91kPa from the negative pressure in device.
In above-mentioned treatment process, it is preferable that in step 4, temperature of the waste water after heat exchange heating is 55-60 DEG C,
Vapor (steam) temperature after flash distillation is 40-45 DEG C；Negative pressure in the two effects separator is -93.94kPa~-83.91kPa.
In above-mentioned treatment process, waste water is steamed under low temperature and condition of negative pressure in an effect separator and two effect separators
Hair, the silica being concentrated in waste water are easier to be precipitated with floccule or particulate form, and the floccule or particulate matter can be with
Solution flowing, without forming hard, fine and close layer of scale in evaporator surface, causes heat exchange efficiency to reduce.
In above-mentioned treatment process, after the concentration of two-effect evaporation unit, there is a large amount of silica to be precipitated, the titanium dioxide
Silicon can be used as the take-away of hydrated SiO 2 product, therefore two-effect evaporation unit concentration process after filtration, washing and drying, in sulphur
Under the premise of sour sodium crystal is undecomposed, two-effect evaporation unit discharges, and the higher the better for sulfur acid sodium amount, can remove greatly in this stage
Silica is measured, the quality of final products anhydrous slufuric acid can be improved.
In above-mentioned treatment process, it is preferable that in step 6, temperature of the filtrate after heat exchange heating is 70-75 DEG C；
The temperature of the steam to heat up through MVR compressor compresses is 80-85 DEG C；Negative pressure in the MVR separator be -83.94kPa~-
53.91kPa。
In above-mentioned treatment process, it is preferable that in step 1, sedimentation separation obtain sediment by filters pressing, filtering,
It is taken out after washing and drying as hydrated SiO 2 product.
In above-mentioned treatment process, it is preferable that Step 2: the cooling water through the cold acquisition of pervaporation is used in step 5
Produce reuse.
In above-mentioned treatment process, it is preferable that in step 4, cooling of the effect flash-off steam in two effect heaters acquisitions
Water is for producing reuse.Not only the cooling cycle water consumption in traditional handicraft had been saved, but also part has been carried out to waste water and has been evaporated, it can be big
Width reduces the cost of wastewater treatment.
In above-mentioned treatment process, it is preferable that in step 5, after the filter cake mashing that filter press filtering obtains is dry
It is taken out as hydrated SiO 2 product.
In above-mentioned treatment process, it is preferable that the condensation in step 6, after the heat source heat exchange cooling of third heat exchanger channels
Water is for producing reuse.
In above-mentioned treatment process, the condensed water of generation as industrial water reuse, make by the precipitation of silica object of generation
For the take-away of hydrated SiO 2 product, the anhydrous sodium sulfate of generation can be used as chemical products take-away, in the process without waste water, solid waste etc.
Waste generates.
Beneficial effects of the present invention:
(1) traditional handicraft is able to solve using processing unit and technique of the invention and dioxy is hydrated to white carbon black and silica gel etc.
Solid waste yield is big in the treatment process of high-salt wastewater containing silica generated in SiClx product sulfuric acid precipitation method production process, transports
It the problem of row bottleneck at high cost, equipment scaling, really realizes the zero-emission of the high-salt wastewater containing silica, makes to be hydrated titanium dioxide
The sulfuric acid precipitation method process changeover of silicon is at process for cleanly preparing；
(2) in treatment process of the invention, high-salt wastewater containing silica is used and adjusts pH by the way that sodium hydroxide is added
Value controls 40~80 DEG C of evaporating temperature to 9~14, make fouling factor silica in evaporation process with floccule or
Grain object form is precipitated, and the floccule or particulate matter can be flowed with solution, without forming hard fouling in evaporator surface
Layer causes heat exchange efficiency to reduce, to eliminate the fouling factor of the high-salt wastewater containing silica in evaporation process, whole process
Medicament is not needed except silica, water treatment agent cost had both been saved, and had in turn avoided the generation of solid waste；
(3) present invention can use low-quality waste heat (such as: ammonium hydroxide waste heat) and be evaporated as heat source to waste water, into
One step reduces the cost of water process；To keep the processing of high-salt wastewater containing silica more feasible and applicable；
(4) due to eliminating the fouling factor in high-salt wastewater containing silica in pre-processing of the present invention, useless
Water steam final when carrying out multiple-effect evaporation can be used evaporation and be cooled down, and cooling medium is useless handled by the present invention
Water had not only saved the cooling cycle water consumption in traditional handicraft, but also has carried out part to waste water and evaporated, and significantly reduced at waste water
The cost of reason；
(5) condensed water that the treatment process generates is as industrial water reuse, and the precipitation of silica object of generation is as water
It closes silica product to take out, the anhydrous sodium sulfate of generation can be used as chemical products take-away, discarded without waste water, solid waste etc. in the process
Object generates.
Referring to following description and accompanying drawings, only certain exemplary embodiments of this invention is disclosed in detail, specifies original of the invention
Reason can be in a manner of adopted.It should be understood that embodiments of the present invention are not so limited in range.In appended power
In the range of the spirit and terms that benefit requires, embodiments of the present invention include many changes, modifications and are equal.For a kind of reality
The feature that the mode of applying is described and/or shown can be made in one or more other embodiments in a manner of same or similar
With, be combined with the feature in other embodiment, or substitution other embodiment in feature.
Detailed description of the invention
Attached drawing described here is only used for task of explanation, and is not intended to limit model disclosed by the invention in any way
It encloses.In addition, shape and proportional sizes of each component in figure etc. are only schematical, it is used to help the understanding of the present invention, and
It is not the specific shape and proportional sizes for limiting each component of the present invention.Those skilled in the art under the teachings of the present invention, can
Implement the present invention to select various possible shapes and proportional sizes as the case may be.
Fig. 1 is SiO in the embodiment of the present invention2The structure of the processing unit of the high-salt wastewater containing silica in sour depositing technology
Schematic diagram；
Fig. 2 is SiO in the embodiment of the present invention2Steaming in sour depositing technology in the processing unit of the high-salt wastewater containing silica
Feel cold structural schematic diagram；
Fig. 3 is SiO in the embodiment of the present invention2It is dry in the processing unit of the high-salt wastewater containing silica in sour depositing technology
The structural schematic diagram of dry machine；
Accompanying drawings symbol description:
1, static mixer；2, subsider；3, it evaporates cold；4, an effect separator；5, an effect heater；6, two effect separation
Device；7, two effect heater；8, filter press；9, MVR separator；10, MVR heater；11, MVR compressor；12, MVR thickener；
13, MVR centrifuge；14, drying machine；15, the first surge tank；16, the second surge tank；17, the first feed pump；18, the first vacuum
Pump；19, an effect forced circulation pump；20, two effect forced circulation pump；21, the second vacuum pump；22, MVR forced circulation pump；23, ponding
Slot；24, feeding spiral conveyer；
201, cooling coil；202, water-spray system；203, dehydrator；204, dehydrator；205, blower；206, import
Valve；207, water circulating pump；208, water circulating pump；209, outlet valve；210, outlet valve；211, collecting-tank；
301, drying machine upper bed body；302, bed body under drying machine；303, drying machine bellows；304, drying machine visor；305,
Drying machine visor；306, drying machine elevator；307, finished product bin.
Specific embodiment
In order to which technical characteristic of the invention, purpose and beneficial effect are more clearly understood, now to skill of the invention
Art scheme carries out described further below, but should not be understood as that limiting the scope of the invention.In the teachings of the present invention
Under, technical staff is contemplated that these are regarded as belonging to the scope of the present invention based on any possible deformation of the invention.
It should be noted that be referred to as " being set to " another element when element, it can directly on the other element or can also
With there are elements placed in the middle.When an element is considered as " connection " another element, it can be directly to another
Element may be simultaneously present centering elements.Term " installation ", " connected ", " connection " shall be understood in a broad sense, for example, it may be
Mechanical connection or electrical connection, the connection being also possible to inside two elements can be directly connected, and can also pass through intermediary
It is indirectly connected, for the ordinary skill in the art, can understand the concrete meaning of above-mentioned term as the case may be.
Term as used herein " vertically ", " horizontal ", "upper", "lower", "left", "right" and similar statement are intended merely to
Bright purpose, is not meant to be the only embodiment.
Unless otherwise defined, all technical and scientific terms used herein and the technical field for belonging to the application
The normally understood meaning of technical staff is identical.The term used in the description of the present application is intended merely to description tool herein
The purpose of the embodiment of body, it is not intended that in limitation the application.Term as used herein "and/or" includes one or more
Any and all combinations of relevant listed item.
Embodiment
This implementation provides a kind of SiO2The processing unit of the high-salt wastewater containing silica in sour depositing technology, as shown in Figure 1,
The processing unit includes pretreatment unit, pre-concentration unit, two-effect evaporation unit, MVR evaporative crystallization unit and drying unit, respectively
Unit, which is sequentially connected, to be connect；
The pretreatment unit includes subsider 2, for the silica in initial gross separation recycling waste water；
The pre-concentration unit includes evaporation cold 3, and preliminary pre-concentration, the steaming are realized in the part evaporation of the moisture for waste water
The elegant loss felt cold is low, < 56kg/h；
The two-effect evaporation unit includes that an effect separator 4, one imitates the effect effect of separator 6, two of heater 5, two 7 and of heater
Filter press 8；The transmission process no consumption energy sets in concentrate Xiang Erxiao separator 6 in the unit waste water one effect separator 4
It is standby, using negative pressure transportation concentrate, additional energy waste will not be generated.
One effect heater 5 is connected to effect 4 phase of a separator circulation, is provided in an effect heater 5 and is connected with external heat source
The first logical heat exchange pipeline, first heat exchange pipeline are provided with inlet and outlet；One effect separator 4 be provided with first gas outlet,
First liquid inlet and the first liquid outlet；Cold 3 are evaporated to be connected with first liquid inlet；
Two effect heaters 7 are connected to two effect 6 phase of separator circulations, are provided in two effect heaters 7 and are connected with external heat source
The second logical heat exchange pipeline, second heat exchange pipeline are provided with inlet and outlet；The first gas outlet and second heat exchange
The import of pipeline is connected；Two effect separators 6 are provided with second gas outlet, second liquid entrance and second liquid outlet；Institute
Second liquid outlet is stated to be connected with filter press 8；First liquid outlet is connected with the second liquid entrance；
As shown in Fig. 2, evaporation cold 3 includes scuttlebutt and the Circulating Pump System that the scuttlebutt periphery is arranged in；It is described
It is provided with blower 205 at the top of scuttlebutt, is successively vertically provided with dehydrator 204, dehydrator 203, water-spray system along blower 205
202, cooling coil 201 and collecting-tank 211；The Circulating Pump System includes two water circulating pumps 207 and 208 in parallel, is followed
The both ends of ring water pump 207 and 208 are connected with outlet valve 209, outlet valve 210 and inlet valve 206, outlet valve 209 and outlet in turn
Valve 210 is connected with dehydrator 204；Inlet valve 206 is connected with collecting-tank 211；The entrance and second gas of cooling coil 201
Outlet is connected；The outlet of cooling coil 201 is connected with the first surge tank 15.
The MVR evaporative crystallization unit includes MVR heater 10, MVR separator 9, MVR compressor 11, MVR thickener 12
With MVR centrifuge 13；
MVR separator 9 is connected to 10 phase of MVR heater circulation, is provided in MVR heater 10 and is connected with external heat source
Third heat exchange pipeline, the third heat exchange pipeline is provided with inlet and outlet；MVR separator 9 is provided with third gas outlet, third
Liquid inlet and third liquid outlet；Third gas outlet, MVR compressor 11 and the third heat exchange pipeline import phase
Connection；Filter press 8 is connected with the third liquid inlet of MVR separator 9；The third liquid outlet and 12 phase of MVR thickener
Connection；MVR thickener 12 is connected with MVR centrifuge 13；
As shown in figure 3, the drying unit includes drying machine 14；Drying machine 14 includes drying machine upper bed body 301, drying machine
Lower bed body 302, drying machine bellows 303, drying machine visor 304 and 305, dry elevator 306 and finished product bin 307；MVR centrifugation
It is provided with feeding spiral conveyer 24 on the pipeline that machine 13 is connected with drying machine upper bed body 301, with drying machine upper bed body
301 are connected；The outlet of bed body 302 is connected with dry elevator 306 under drying machine；Dry elevator 306 and finished product bin
307 are connected；The lateral wall of bed body 302 under drying machine is arranged in drying machine visor 304 and 305, and the setting of drying machine bellows 303 exists
The bottom of bed body 302 under drying machine.
The inlet and outlet of first heat exchange pipeline of one effect heater 5 are for being connected to the cyclic ammonia water stream of extraneous coking workshop section.
In a preferred embodiment, pre-concentration unit further includes the first surge tank 15；First surge tank 15 is for receiving
Collection and the condensed water of storage evaporation cold 3 produce reuse；First surge tank 15 is provided with the first vacuum pump 18.The MVR evaporation knot
Brilliant unit further includes the second surge tank 16；Second surge tank 16 is used to collect and store the cold of the outlet of the third heat exchange pipeline
Condensate produces reuse；Second surge tank 16 is provided with the second vacuum pump 21.
In a preferred embodiment, the is provided on cold 3 pipeline that is connected with first liquid inlet of evaporation
One feed pump 17；An effect forced circulation pump 19 is provided on the pipeline that one effect heater 5 is connected to effect 4 phase of a separator circulation；
Two effect forced circulations 20 are provided on the pipeline that two effect heaters 7 are connected to two effect 6 phase of separator circulations；MVR separator 9 with
MVR forced circulation pump 22 is provided on the pipeline of 10 phase of MVR heater circulation connection.
This implementation also provides a kind of SiO2The treatment process of the high-salt wastewater containing silica in sour depositing technology is to use
What above-mentioned processing unit carried out, comprising the following steps:
Step 1, bin cure acid precipitation method hydrated SiO 2 in future produce the (85t/ of high-salt wastewater containing silica of workshop section
H) mixing with sodium hydroxide and adjusting pH value of waste water is 9-10, and the flocculation of the fouling factor enters sedimentation after static mixer mixes
In slot 2 and sedimentation separation is carried out, obtains sediment and supernatant effluent；
Wherein, sediment by filters pressing, be filtered, washed and dried after as hydrated SiO 2 product take out；
Supernatant effluent is sent into evaporation cold 3 and is used as the recirculated cooling water for evaporating cold cooling steam, in cooling by step 2
During steam, supernatant effluent has also carried out part and has evaporated, and realizes preliminary pre-concentration；Evaporate the evaporating temperature in cold 3
It is 40-80 DEG C, negative pressure is -93.94kPa~-53.91kPa；The cooling water that cold 3 obtain is evaporated to send to white carbon black workshop as life
Fisheries water；
Step 3, the waste water (70t/h) by preliminary pre-concentration are sent by the first feed pump 17 of two-effect evaporation unit
Into an effect separator 4, circulation is beaten by an effect forced circulation pump 19, is exchanged heat via an effect heater 5, an effect heater
In the first heat exchanger channels heat source from the cyclic ammonia water of coking workshop section (temperature be 75-85 DEG C)；The waste water of preliminary pre-concentration
It is flashed in Yu Yixiao separator 4 after heat exchange is warming up to about 60-65 DEG C；One effect separator 4 in negative pressure be-
83.94kPa~-53.91kPa；
Step 4, the waste liquid after effect 4 flash concentration of separator enter in two effect separators 6, are forced by two effects
Circulating pump 20 beats circulation, is exchanged heat again via two effect heaters 7, the heat source of the second heat exchanger channels in two effect heaters 7
Steam (about 55-60 DEG C) after an effect flash distillation of separator 4；Waste water is after heat exchange is warming up to about 45-50 DEG C in two effects point
From being flashed in device 6；Negative pressure in two effect separators 6 is -93.94kPa~-83.91kPa；
Step 5, the waste water after two effect 6 flash concentrations of separator enter filtering in filter press 8 and obtain filter cake and filter
Liquid；It is taken out after filter cake mashing is dry as hydrated SiO 2 product；Steam (about 40-45 DEG C) after the two effect flash distillations of separators 6
It carries out being condensed back to sending and receiving to white carbon black workshop as industrial water into evaporating in cold 3；
Step 6, filtrate (30t/h) enters in MVR separator 9, by MVR forced circulation pump 22 via MVR heater 10
It exchanges heat, the steam that the heat sources of the third heat exchanger channels in MVR heater 10 is flashed from MVR separator 9 is through MVR compressor
The steam (about 80-85 DEG C) of 11 compression heatings；Filtrate by heat exchange be warming up to about 70-75 DEG C and via water storage tank 23 after, in MVR
It is flashed in separator 9；Negative pressure in MVR separator 9 is -62.7~-83.91kPa；The heat source of third heat exchanger channels exchanges heat
Condensed water after cooling is for producing reuse；
Step 7, is precipitated sodium sulfate crystal after 9 flash concentration of MVR separator, and sodium sulphate magma is big due to density
And the lower part salt leg for being settled down to MVR separator 9 is enriched with, the sodium sulphate magma after enrichment is into MVR thickener 12 into one
Enter in the MVR centrifuge 13 of Double -stagepusher formula after step concentration thickening and be centrifuged, is centrifugally separating to obtain moisture percentage
About 5% sodium sulphate is delivered in internal heating fluidized bed drying machine 14 by feeding spiral conveyer 24 and is dried in dry packing
Process completes dry, packaging, and it is outer to can be used as the progress of industrial sulphuric acid sodium for finally obtained anhydrous slufuric acid sodium content >=98.5%
It sells.
Multiple element, ingredient, component or step can be provided by single integrated component, ingredient, component or step.Optionally
Ground, single integrated component, ingredient, component or step can be divided into multiple element, ingredient, component or the step of separation.It is used to
The open "a" or "an" for describing element, ingredient, component or step is not said to exclude other elements, ingredient, component
Or step.
The above embodiments merely illustrate the technical concept and features of the present invention, and its object is to allow person skilled in the art
Scholar cans understand the content of the present invention and implement it accordingly, and it is not intended to limit the scope of the present invention.It is all according to the present invention
Equivalent change or modification made by Spirit Essence, should be covered by the protection scope of the present invention.
Claims (10)
1. a kind of SiO2The processing unit of the high-salt wastewater containing silica in sour depositing technology, it is characterised in that: the processing unit packet
Pretreatment unit, pre-concentration unit, two-effect evaporation unit, MVR evaporative crystallization unit and drying unit, each unit is included to be sequentially connected
It connects；
The pretreatment unit includes subsider, for the silica in initial gross separation recycling waste water；
The pre-concentration unit includes evaporating cold, the preliminary pre-concentration of part evaporation realization of the moisture for waste water；
The two-effect evaporation unit includes an effect separator, an effect heater, two effect separators, two effect heaters and filter press；
The one effect heater is mutually recycled and is connected to the effect separator, and described one imitates and is provided in heater and external heat source
The first heat exchange pipeline being connected, first heat exchange pipeline are provided with inlet and outlet；The one effect separator is provided with the first gas
Body outlet, the first liquid inlet and the first liquid outlet；The evaporation is cold to be connected with first liquid inlet；
The two effect heater is mutually recycled and is connected to the two effects separator, and described two imitate and are provided in heater and external heat source
The second heat exchange pipeline being connected, second heat exchange pipeline are provided with inlet and outlet；The first gas outlet and described second
The import of heat exchange pipeline is connected；The two effects separator is provided with second gas outlet, second liquid entrance and second liquid
Outlet；The second liquid outlet is connected with the filter press；First liquid outlet and the second liquid entrance phase
Connection；Cold be connected is evaporated with described in the second gas outlet；
The MVR evaporative crystallization unit includes MVR heater, MVR separator, MVR compressor, MVR thickener and MVR centrifugation
Machine；
The MVR separator is mutually recycled with the MVR heater and is connected to, and is provided in the MVR heater and external heat source phase
The third heat exchange pipeline of connection, the third heat exchange pipeline are provided with inlet and outlet；The MVR separator is provided with third gas and goes out
Mouth, third liquid inlet and third liquid outlet；The third gas outlet, the MVR compressor and the third heat exchanger tube
The import in road is connected；The filter press is connected with the third liquid inlet of the MVR separator；The third liquid outlet
It is connected with the MVR thickener；The MVR thickener is connected with the MVR centrifuge；
The drying unit includes drying machine；The MVR centrifuge is connected with the drying machine.
2. processing unit according to claim 1, it is characterised in that: it is described one effect heater the first heat exchange pipeline into
Export the cyclic ammonia water stream for being connected to extraneous coking workshop section.
3. processing unit according to claim 1, it is characterised in that: the pre-concentration unit further includes the first surge tank；
First surge tank is used to collect and store the cold condensed water production reuse of the evaporation；
Preferably, first surge tank is provided with the first vacuum pump.
4. processing unit according to claim 1, it is characterised in that: the MVR evaporative crystallization unit further includes second slow
Rush tank；Second surge tank is used to collect and store the condensed water production reuse of the outlet of the third heat exchange pipeline；
Preferably, second surge tank is provided with the second vacuum pump.
5. processing unit according to claim 1, it is characterised in that: the evaporation is cold to be connected with first liquid inlet
The first feed pump is provided on logical pipeline；
Preferably, an effect heater mutually recycles with the effect separator and is provided with an effect forced circulation on the pipeline being connected to
Pump；
Preferably, the two effect heater mutually recycles with the two effects separator and is provided with two effect forced circulations on the pipeline being connected to
Pump；
Preferably, the MVR separator mutually recycles with the MVR heater and is provided with MVR forced circulation pump on the pipeline being connected to.
6. processing unit according to claim 1, it is characterised in that: the cold evaporation includes scuttlebutt and setting described
The Circulating Pump System of scuttlebutt periphery；
It is provided with blower at the top of the scuttlebutt, is successively vertically provided with dehydrator, water-spray system, cooler pan along the blower
Pipe and collecting-tank；
The Circulating Pump System includes two water circulating pumps in parallel, and the both ends of the water circulating pump are connected with outlet valve in turn
And inlet valve, the outlet valve are connected with the dehydrator；The inlet valve is connected with the collecting-tank；
The entrance of the cooling coil is connected with second gas outlet.
7. processing unit according to claim 1, it is characterised in that: the drying machine includes drying machine upper bed body, drying
Bed body, drying machine bellows, drying machine visor, dry elevator and finished product bin under machine；
The MVR centrifuge is connected with the drying machine upper bed body；The outlet of bed body is mentioned with the drying under the drying machine
The machine of liter is connected；The dry elevator is connected with the finished product bin；The drying machine visor is arranged in the drying machine
The bottom of bed body under the drying machine is arranged in the lateral wall of lower bed body, the drying machine bellows；
Preferably, feed auger conveying is additionally provided on the pipeline that the MVR centrifuge is connected with the drying machine upper bed body
Machine.
8. a kind of SiO2The treatment process of the high-salt wastewater containing silica in sour depositing technology is any using claim 1-7
The item processing unit carries out, comprising the following steps:
Step 1, bin cure acid precipitation method hydrated SiO 2 in future produce the high-salt wastewater containing silica and sodium hydroxide of workshop section
It is alkalinity that mixing, which adjusts pH value of waste water, and carries out sedimentation separation, obtains sediment and supernatant effluent；
Supernatant effluent is sent to evaporating to be used as in cold and evaporates the recirculated cooling water of cold cooling steam, in cooling steam by step 2
During, supernatant effluent has also carried out part and has evaporated, and realizes preliminary pre-concentration；
Step 3, the waste water by preliminary pre-concentration enter in an effect separator, are added by an effect forced circulation pump via an effect
Hot device exchanges heat, and the heat source of the first heat exchanger channels in an effect heater is from the cyclic ammonia water of coking workshop section；It is preliminary pre- dense
The waste water of contracting is flashed in Yu Yixiao separator after heat exchange heating；
Step 4, the waste liquid after an effect separator flash concentration enter in two effect separators, pass through two effect forced circulation pumps
It is exchanged heat again via two effect heaters, the heat source of the second heat exchanger channels in two effect heaters is from an effect separator flash distillation
Steam afterwards；Waste water is flashed in Yu Erxiao separator after heat exchange heating, and an effect flash-off steam is in two effect heaters
Condensation is carried out to be recycled；
Step 5, the waste water after two effect separator flash concentrations enter filtering in filter press and obtain filter cake and filtrate；Two effects
Steam after separator flash distillation enters the cold unit of evaporation and carries out condensing recovery utilization；
Step 6, filtrate enter in MVR separator, are exchanged heat by MVR forced circulation pump via MVR heater, MVR heating
Steam of the heat source of third heat exchanger channels in device from the steam that MVR separator flashes after the heating of MVR compressor compresses；Filter
Liquid is flashed in MVR separator after heat exchange heating, and flash-off steam carries out condensation recycling benefit in MVR heater
With；
Step 7, the sodium sulfate crystal being precipitated after MVR separator flash concentration successively pass through MVR thickener, MVR centrifuge
With solid sodium sulfate is obtained after drying machine.
9. treatment process according to claim 8, it is characterised in that: in step 1, sodium hydroxide is added and adjusts waste water
PH value be 9-14, preferable ph 9-10；
Preferably, in step 2, the evaporating temperature of preliminary pre-concentration is 40-80 DEG C；Negative pressure be -93.94kPa~-
53.91kPa；
Preferably, in step 3, the temperature of the cyclic ammonia water is 70-80 DEG C, and the waste water of preliminary pre-concentration rises by heat exchange
Temperature after temperature is 60-65 DEG C；Vapor (steam) temperature after flash distillation is 55-60 DEG C；It is described one effect separator in negative pressure be-
83.94kPa~-53.91kPa；
Preferably, in step 4, temperature of the waste water after heat exchange heating is 55-60 DEG C, and the vapor (steam) temperature after flash distillation is 40-
45℃；Negative pressure in the two effects separator is -95.94kPa~-83.91kPa；
Preferably, in step 6, temperature of the filtrate after heat exchange heating is 70-75 DEG C；It heats up through MVR compressor compresses
The temperature of steam is 80-85 DEG C；Negative pressure in the MVR separator is -83.94kPa~-53.91kPa.
10. treatment process according to claim 8, it is characterised in that: in step 1, the sediment of sedimentation separation acquisition
By filters pressing, be filtered, washed and dried after as hydrated SiO 2 product take out；
Preferably, Step 2: the cooling water through the cold acquisition of pervaporation is for producing reuse in step 5；
Preferably, in step 4, an effect flash-off steam is used to produce reuse in the cooling water that two effect heaters obtain；
Preferably, in step 5, hydrated SiO 2 product is used as after the filter cake mashing that filter press filtering obtains is dry
It takes out；
Preferably, in step 6, the condensed water after the heat source heat exchange cooling of third heat exchanger channels is for producing reuse.
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