CN113082846A - Impurity-removing and purifying process and purifying device for alkaline residue of ammonia-soda plant - Google Patents
Impurity-removing and purifying process and purifying device for alkaline residue of ammonia-soda plant Download PDFInfo
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- CN113082846A CN113082846A CN202110323879.3A CN202110323879A CN113082846A CN 113082846 A CN113082846 A CN 113082846A CN 202110323879 A CN202110323879 A CN 202110323879A CN 113082846 A CN113082846 A CN 113082846A
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- 238000000034 method Methods 0.000 title claims description 9
- 239000002002 slurry Substances 0.000 claims abstract description 161
- 239000002562 thickening agent Substances 0.000 claims abstract description 77
- 239000007787 solid Substances 0.000 claims abstract description 54
- 238000000746 purification Methods 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000003513 alkali Substances 0.000 claims abstract description 31
- 239000010881 fly ash Substances 0.000 claims abstract description 30
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims abstract description 25
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 24
- 239000012535 impurity Substances 0.000 claims abstract description 22
- 230000003750 conditioning effect Effects 0.000 claims abstract description 20
- 239000011268 mixed slurry Substances 0.000 claims abstract description 20
- 239000012065 filter cake Substances 0.000 claims abstract description 18
- 239000013505 freshwater Substances 0.000 claims abstract description 14
- 230000018044 dehydration Effects 0.000 claims abstract description 10
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 10
- 239000008394 flocculating agent Substances 0.000 claims abstract description 10
- 239000003518 caustics Substances 0.000 claims description 35
- 239000010802 sludge Substances 0.000 claims description 35
- 239000000706 filtrate Substances 0.000 claims description 23
- 150000001875 compounds Chemical class 0.000 claims description 12
- 229910000831 Steel Inorganic materials 0.000 claims description 11
- 239000010959 steel Substances 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 10
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 241000196324 Embryophyta Species 0.000 description 19
- 239000002893 slag Substances 0.000 description 12
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 10
- 230000005540 biological transmission Effects 0.000 description 9
- 238000011010 flushing procedure Methods 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 7
- 239000002699 waste material Substances 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 6
- 229910000019 calcium carbonate Inorganic materials 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 235000017166 Bambusa arundinacea Nutrition 0.000 description 4
- 235000017491 Bambusa tulda Nutrition 0.000 description 4
- 241001330002 Bambuseae Species 0.000 description 4
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 4
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 4
- 239000011425 bamboo Substances 0.000 description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000005065 mining Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- 210000005056 cell body Anatomy 0.000 description 3
- 238000013016 damping Methods 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 235000017550 sodium carbonate Nutrition 0.000 description 3
- 239000002689 soil Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 238000009621 Solvay process Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- CYUOWZRAOZFACA-UHFFFAOYSA-N aluminum iron Chemical compound [Al].[Fe] CYUOWZRAOZFACA-UHFFFAOYSA-N 0.000 description 1
- 238000009412 basement excavation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- -1 salt chloride Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
- B01D36/04—Combinations of filters with settling tanks
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention discloses an impurity removal and purification process and a purification device for alkaline residue in an ammonia-soda plant, which comprises the following steps: adopting a cutter suction dredger to collect and dig the alkaline residue slurry in the alkaline residue field, conveying the alkaline residue slurry to a primary high-efficiency thickener through a slurry feeding pipe, adding a flocculating agent into the slurry feeding pipe at multiple points, conveying the slurry to a secondary high-efficiency thickener, conveying the slurry to a conditioning tank, and adding fresh water and fly ash to prepare mixed slurry with the solid mass content of 10-20%; and (3) feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content reduced to below 0.5%, the sulfate ion content reduced to below 0.2% and the water content reduced to below 45%. According to the invention, the inorganic polymeric flocculant is added, so that the alkali residue slurry entering the high-efficiency thickener forms large floccules, and the working efficiency of the thickener is greatly improved. The purification process can efficiently, economically and massively remove the alkaline residue in the alkaline residue field, and effectively solve the problem of large-scale stockpiling of the alkaline residue.
Description
Technical Field
The invention relates to the technical field of caustic sludge treatment. More specifically, the invention relates to an impurity removal and purification process and a purification device for alkaline residue in an ammonia-soda plant.
Background
The method for preparing sodium carbonate by ammonia-soda process uses about 1.5t of raw salt per ton of soda, the total utilization rate is only 29%, and the rest is discarded. To decompose NH4Cl makes ammonia recycle, lime milk (Ca (OH) is added into the system2) Distilling ammonia, CaCl generated in the process2、CaCO3SiO with limestone2、CaCO3And a small amount of impurities not removed by the crude salt are discharged from the bottom of the distillation column. In addition, primary and secondary slimes refined from brine, with Mg (OH)2And CaCO3The amount of the salt is mainly determined by the content of the original salt, and the salt should be treated together when the amount is different from plant to plant. The composition of the waste liquid was roughly: CaCl2 90～120g/L、NaCl45～55g/L、CaCO 3 10～20g/L、CaO 2～4g/L、Mg(OH)2 3～10g/L、SiO21-5 g/L. The quantity and composition of the waste residue vary with the raw materials, but the difference between plants is not great, and the main components of the waste residue are calcium carbonate and soluble salt chloride which are well known in the scientific field.
In each large alkali factory for producing soda by ammonia-soda process in China, a large amount of discharged caustic sludge is piled up, and cannot be reasonably treated and utilized for a long time, so that not only is resource waste caused, but also a large amount of manpower, material resources and financial resources are consumed for management, land occupation is caused, environment is polluted, and ecological balance is damaged, therefore, the treatment of the caustic sludge is always a bottleneck for restricting the development of soda industry. Along with the soundness of national environmental governance policy and regulations, various soda plants and research and design units in China are mutually matched, so that a large amount of work is performed on reasonable discharge and comprehensive utilization of waste liquor and waste residue of soda ash, and certain achievements are obtained. Various enterprises utilize waste residues to build a dam, build a new slag yard or fill a sea to build a land, be used as engineering backfill, build a road and fill a pad soil (non-main road) and the like at a reclamation dam of a sea beach, but have a plurality of risks: soluble salts are easy to dissolve and run off after long-term leaching, and can cause engineering problems such as collapse and the like; the alkaline residue soil has high thixotropy, is easy to dry in air and pulverize, so that local foundation or roadbed softening is generated, and the strength and the bearing capacity are reduced. In addition, the caustic sludge is used as a raw material to develop byproducts, such as silicate bricks, bubble concrete blocks, soil conditioners (or called calcium magnesium fertilizers and calcium fertilizers), building cementing materials (cement), flue gas desulfurization agents and the like, but the caustic sludge has the technical problems of high water content, difficult chloride reduction, difficult paste and mud separation and the like, and is limited by a plurality of factors such as economic cost, market development and the like, so that the caustic sludge is mostly in a research stage at present, is not produced in a large scale, and cannot meet the requirements of large-scale and efficient treatment and utilization.
Disclosure of Invention
An object of the present invention is to solve at least the above problems and to provide at least the advantages described later.
The invention also aims to provide an impurity removal and purification process for the alkaline residue in the ammonia-soda plant, which comprises the steps of forming the accumulated alkaline residue into alkaline residue slurry with the water content of 50-90% by hydraulic flushing, mining and digging the alkaline residue slurry in the alkaline residue plant by a cutter suction dredger, adding fresh water and fly ash for conditioning, and conveying the alkaline residue slurry into a diaphragm plate-and-frame filter press for filter pressing to obtain the alkaline residue filter cake meeting the requirements. According to the invention, the inorganic polymeric flocculant is added, so that the alkali residue slurry entering the thickener forms large floccules, and the working efficiency of the thickener is greatly improved. The purification process can efficiently, economically and massively remove the alkaline residue in the alkaline residue field, and effectively solve the problem of large-scale stockpiling of the alkaline residue.
To achieve these objects and other advantages in accordance with the present invention, there is provided a process for the decontamination and purification of soda ash from an ammonia-soda plant, comprising the steps of:
s1, adopting a cutter suction dredger to collect alkaline residue slurry in an alkaline residue field, conveying the alkaline residue slurry to a first-level efficient thickener through a slurry feeding pipe, and adding a flocculating agent into the slurry feeding pipe at multiple points to obtain first concentrated slurry, wherein the mass content of alkaline residue in the first concentrated slurry is 25-35%;
s2, conveying the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 25-35%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash to prepare mixed slurry with the solid mass content of 10-20%;
and S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content reduced to below 0.5%, the sulfate ion content reduced to below 0.2% and the water content reduced to below 45%, and discharging the filtrate to a secondary high-efficiency thickener through a filtrate outlet header pipe.
Preferably, the caustic sludge slurry in the step S1 is formed by hydroexcavation of caustic sludge deposited in a caustic sludge field, the solid mass content of the caustic sludge slurry is 8-20%, and the caustic sludge deposited in the caustic sludge field coexists in a solid state, a semi-solid state and a liquid state.
Preferably, the flocculating agent in the step S1 is one or more of polymeric ferric sulfate, polymeric aluminum sulfate and polymeric aluminum ferric silicate.
Preferably, the mass ratio of the flocculant to the solid in the alkaline residue slurry in step S1 is (1-5 kg): 1 t.
Preferably, in the step S1, the flocculant is prepared into a flocculant solution with a mass content of 10% -30%, and the volume ratio of the flocculant solution to the alkali residue slurry is (1-10 mL): 1L of the compound.
Preferably, the first-stage high-efficiency thickener and the second-stage high-efficiency thickener respectively comprise one of a high-efficiency deep cone thickener and an inclined plate thickener.
Preferably, the mass ratio of the fly ash to the solids in the second concentrated slurry is (20-200 kg): 1 t.
Preferably, fresh water is added into the fly ash to prepare fly ash slurry with the mass content of 10-20%, and the volume ratio of the fly ash slurry to the alkaline residue slurry is (20-100 mL): 1L of the compound.
The invention provides a purification device for an impurity removal and purification process of alkaline residue in an ammonia-soda plant, which comprises the following components: the device comprises a twisting suction ship, a slurry feeding pipe, a primary high-efficiency thickener, a conditioning tank, a diaphragm plate and frame filter press and a secondary high-efficiency thickener, wherein one end of the slurry feeding pipe is communicated with the twisting suction ship, the other end of the slurry feeding pipe is communicated with the primary high-efficiency thickener, the primary high-efficiency thickener is communicated with the secondary high-efficiency thickener, the secondary high-efficiency thickener is communicated with the conditioning tank, the conditioning tank is communicated with the diaphragm plate and frame filter press, and the diaphragm plate and frame filter press discharges filtrate into the secondary high-efficiency thickener.
Preferably, a plurality of adding holes are formed in the pulp feeding pipe at intervals, each adding hole is vertically inserted into a steel pipe, the feed end of each steel pipe is funnel-shaped, and the feed end of each steel pipe corresponds to one opening of the flocculant adding pipe;
the pulp feeding pipe is perpendicular to the primary high-efficiency thickener and is connected with the central feeding cylinder.
The invention at least comprises the following beneficial effects:
the alkali residue slurry entering the thickener forms large floccules by adding the inorganic polymeric flocculant, so that the working efficiency of the thickener is greatly improved;
the process device adopts the high-efficiency thickener, has the advantages of continuous operation, stable and reliable production, low energy consumption, simple operation and the like compared with other concentration equipment, realizes the alkali residue pulping and concentration process for many times by the serial use of the high-efficiency thickener, and greatly reduces the impurity content in the alkali residue;
the physical property of the alkaline residue is improved by the doped fly ash, so that the alkaline residue slurry treated by the diaphragm plate-and-frame filter press is fully dehydrated to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 1%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, and the subsequent utilization is facilitated;
the process can efficiently, economically and massively remove the alkaline residue in the alkaline residue field, and effectively solve the problem of large-scale stockpiling of the alkaline residue.
Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention.
Drawings
FIG. 1 is a schematic structural diagram of a purification device for the impurity removal and purification process of alkaline residue in an ammonia-soda plant according to the present invention;
fig. 2 is a schematic structural diagram of the primary high-efficiency thickener and the secondary high-efficiency thickener of the invention.
Reference numerals: a pulp feeding pipe 1, a central feeding cylinder 3, a material distribution disc 4, a transmission device 5, a transmission shaft 6, a rake frame 7, a tank body 8, a flocculating agent adding pipe 9 and a damping plate 10
Detailed Description
The invention provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, adopting a cutter suction dredger to collect and dig the alkaline residue slurry in the alkaline residue field, conveying the alkaline residue slurry to a first-level efficient thickener through a slurry supply pipe 1, and adding a flocculating agent into the slurry supply pipe 1 at multiple points to ensure that the alkaline residue slurry and the flocculating agent are fully mixed as early as possible to obtain concentrated slurry, wherein the mass content of the alkaline residue in the concentrated slurry is 25-35%; the clear overflow water returns to the caustic sludge field for hydraulic excavation or is discharged after treatment.
S2, conveying the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 25-35%; the clear overflow water is returned to the caustic sludge field for hydraulic flushing or discharged after treatment through filtrate washing discharged from the filtrate outlet header pipe.
S3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash to prepare mixed slurry with the solid mass content of 10-20%;
and S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content reduced to below 0.5%, the sulfate ion content reduced to below 0.2% and the water content reduced to below 45%, discharging the filtrate to a secondary high-efficiency thickener through a filtrate outlet header pipe, and returning the clarified overflow water to an alkaline residue field for hydraulic flushing or discharging after treatment.
The caustic sludge slurry in the step S1 is formed by hydroexcavation of caustic sludge deposited in a caustic sludge field, the caustic sludge deposited in the caustic sludge field coexists in a solid state, a semi-solid state and a liquid state, and has a water content of 50% to 90%.
The flocculating agent in the step S1 is one or more of polymeric ferric sulfate, polymeric aluminum sulfate and polymeric aluminum ferric silicate.
In the step S1, the mass ratio of the flocculant to the solid in the alkaline residue slurry is (1-5 kg): 1 t;
or step S1, preparing the flocculant into a flocculant solution with the mass content of 10% -30%, wherein the volume ratio of the flocculant solution to the alkali residue slurry is (110 mL): 1L of the compound.
The first-stage high-efficiency thickener and the second-stage high-efficiency thickener respectively comprise one of a high-efficiency deep cone thickener and an inclined plate thickener.
The mass ratio of the fly ash to the solid in the second concentrated slurry is (20-200 kg): 1 t;
or adding fresh water into the fly ash to prepare fly ash slurry with the mass content of 10-20%, wherein the volume ratio of the fly ash slurry to the alkali slag slurry is (20-100 mL): 1L of the compound.
The invention provides a purification device for an impurity removal and purification process of alkaline residue in an ammonia-soda plant, which comprises the following components: the device comprises a twisting and sucking ship, a slurry feeding pipe 1, a primary high-efficiency thickener, a conditioning tank, a diaphragm plate and frame filter press and a secondary high-efficiency thickener, wherein one end of the slurry feeding pipe 1 is communicated with the twisting and sucking ship, the other end of the slurry feeding pipe is communicated with the primary high-efficiency thickener, the primary high-efficiency thickener is communicated with the secondary high-efficiency thickener, the secondary high-efficiency thickener is communicated with the conditioning tank, the conditioning tank is communicated with the diaphragm plate and frame filter press, and the diaphragm plate and frame filter press discharges filtrate into the secondary high-efficiency thickener.
A plurality of adding holes are formed in the pulp feeding pipe 1 at intervals, each adding hole is vertically inserted into a steel pipe, the feed end of each steel pipe is funnel-shaped, and the feed end of each steel pipe corresponds to one opening of the flocculant adding pipe 9; the outer diameter of the steel pipe is just matched with the diameter of the adding hole, and the steel pipe can be inserted into the adding hole.
The pulp feeding pipe 1 is perpendicular to the primary high-efficiency thickener, and the pulp feeding pipe 1 is connected with the central feeding cylinder 3;
high-efficient thickener of one-level includes central feeding section of thick bamboo 3, branch charging tray 4, transmission 5, transmission shaft 6, harrow frame 7, cell body 8, damping plate 10, transmission shaft 6 sets up 8 central point of cell body puts, and by transmission 5 drive rotates, the cover is equipped with central feeding section of thick bamboo 3 on the transmission shaft 6, 3 inboards of central feeding section of thick bamboo are provided with damping plate 10, divide charging tray 4 to set up on the transmission shaft 6 and be located the below of central feeding section of thick bamboo 3, harrow frame 7 sets up the end of transmission shaft 6 just is located 8 bottoms of cell body.
The pulp feeding pipe 1 is arranged below the overflow surface of the high-efficiency thickener. The slurry feeding pipe 1 enters the central feeding cylinder 3 in a single pipe or a double pipe from the tangential direction. The addition hole of the flocculating agent is arranged on the pulp feeding pipe 1.2 adding holes on the pulp feeding pipe 1 are respectively made of 2 stainless steel pipes with the specification of 20mm, the feeding end of each stainless steel pipe is a funnel, the other end of each stainless steel pipe is inserted into the pulp feeding pipe 1 by 50mm, the horizontal distance of the 2 adding holes is 2m, and the height difference between the funnels is 100 mm.
The present invention is further described in detail below with reference to examples so that those skilled in the art can practice the invention with reference to the description.
It is to be noted that the experimental methods described in the following embodiments are all conventional methods unless otherwise specified, and the reagents and materials are commercially available unless otherwise specified.
< example 1>
The embodiment provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, carrying out hydraulic flushing on the alkali slag deposited in the alkali slag field to form alkali slag slurry, adopting a cutter suction dredger to pick and dig the alkali slag slurry in the alkali slag field, wherein the solid mass content of the alkali slag slurry is 8%, the water content is 50.2%, the chloride ion content is 6.8%, the sulfate ion content is 1.2%, the alkali slag deposited in the alkali slag field coexists in a solid state, a semi-solid state and a liquid state, conveying the alkali slag to a first-stage high-efficiency thickener through a slurry feeding pipe 1, and adding polymeric ferric sulfate into the slurry feeding pipe 1 at multiple points to obtain first concentrated slurry, wherein the alkali slag mass content in the first concentrated slurry is 25.1%; the mass ratio of the flocculant to the solid in the alkaline residue slurry is 5 kg: 1 t;
s2, sending the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 28.3%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash, and preparing into mixed slurry with the solid mass content of 10.0%; the mass ratio of the fly ash to the solids in the concentrated slurry is 20 kg: 1 t;
s4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 0.5%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, wherein the water content of the alkaline residue filter cake is 44.7%, the chloride ion content is 0.7%, the sulfate ion content is 0.15%, and the filtrate is discharged to a second-stage high-efficiency thickener through a filtrate outlet header pipe.
< example 2>
The embodiment provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, carrying out hydraulic flushing on the alkaline residue deposited in the alkaline residue field to form alkaline residue slurry, mining the alkaline residue slurry in the alkaline residue field by using a cutter suction dredger, wherein the alkaline residue deposited in the alkaline residue field coexists in a solid state, a semi-solid state and a liquid state, the solid mass content of the alkaline residue slurry is 10.6%, the water content is 61%, the chloride ion content is 8.2%, and the sulfate ion content is 0.9%, conveying the alkaline residue slurry to a first-stage high-efficiency thickener through a slurry feeding pipe 1, and adding polymeric aluminum sulfate into the slurry feeding pipe 1 at multiple points to obtain first concentrated slurry, wherein the alkaline residue mass content in the first concentrated slurry is 26.7%; the mass ratio of the flocculant to the solid in the alkaline residue slurry is 3 kg: 1 t.
S2, conveying the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 26%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash, and preparing a mixed slurry with a solid mass content of 11.6%; the mass ratio of the fly ash to the solid in the concentrated slurry is 100 kg: 1 t.
S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 0.5%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, wherein the water content of the alkaline residue filter cake is 44.1%, the chloride ion content is 0.6%, the sulfate ion content is 0.1%, and the filtrate is discharged to a second-stage high-efficiency thickener through a filtrate outlet header pipe.
< example 3>
The embodiment provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, carrying out hydraulic flushing on the alkaline residue deposited in the alkaline residue field to form alkaline residue slurry, adopting a cutter suction dredger to pick and dig the alkaline residue slurry in the alkaline residue field, wherein the solid mass content of the alkaline residue slurry is 13.5%, the water content of the alkaline residue slurry is 68%, the chloride ion content of the alkaline residue slurry is 7.4%, the sulfate ion content of the alkaline residue slurry is 0.8%, the alkaline residue deposited in the alkaline residue field coexists in a solid state, a semi-solid state and a liquid state, the water content of the alkaline residue slurry is 50% -90%, conveying the alkaline residue slurry to a first-stage efficient thickener through a slurry feeding pipe 1, and adding aluminum ferric polysilicate into the slurry feeding pipe 1 at multiple points to obtain first concentrated slurry, wherein the alkaline residue mass content of the first concentrated slurry is; the mass ratio of the flocculant to the solid in the alkaline residue slurry is 1 kg: 1 t.
S2, sending the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 30.5%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash, and preparing into mixed slurry with the solid mass content of 13.4%; the mass ratio of the fly ash to the solids in the concentrated slurry is 200 kg: 1 t.
S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 0.5%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, wherein the water content of the alkaline residue filter cake is 43.0%, the chloride ion content is 0.5%, the sulfate ion content is 0.08%, and the filtrate is discharged to a second-stage high-efficiency thickener through a filtrate outlet header pipe.
< example 4>
The embodiment provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, carrying out hydraulic flushing on the alkaline residue deposited in the alkaline residue field to form alkaline residue slurry, mining the alkaline residue slurry in the alkaline residue field by using a cutter suction dredger, wherein the solid mass content of the alkaline residue slurry is 15.2%, the water content is 77%, the chloride ion content is 8.7%, the sulfate ion content is 1.4%, the alkaline residue deposited in the alkaline residue field coexists in a solid state, a semi-solid state and a liquid state, conveying the alkaline residue to a first-stage high-efficiency thickener through a slurry feeding pipe 1, and adding polymeric aluminum sulfate into the slurry feeding pipe 1 at multiple points to obtain first concentrated slurry, wherein the alkaline residue mass content in the first concentrated slurry is 31.5%; the mass ratio of the flocculant to the solid in the alkaline residue slurry is 10 mL: 1L of the compound.
S2, sending the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 32.7%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash, and preparing into mixed slurry with the solid mass content of 17.9%; the mass ratio of the fly ash to the solid in the concentrated slurry is 20 mL: 1L of the compound.
S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 0.5%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, wherein the water content of the alkaline residue filter cake is 44.2%, the chloride ion content is 0.8%, the sulfate ion content is 0.16%, and the filtrate is discharged to a second-stage high-efficiency thickener through a filtrate outlet header pipe.
< example 5>
The embodiment provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, carrying out hydraulic flushing on the alkaline residue deposited in the alkaline residue field to form alkaline residue slurry, adopting a cutter suction dredger to pick and dig the alkaline residue slurry in the alkaline residue field, wherein the solid mass content of the alkaline residue slurry is 17.9%, the water content is 82%, the chloride ion content is 9.2%, the sulfate ion content is 1.1%, the alkaline residue deposited in the alkaline residue field coexists in a solid state, a semi-solid state and a liquid state, the water content is 50% -90%, conveying the alkaline residue to a first-stage high-efficiency thickener through a slurry feeding pipe 1, and adding polysilicate aluminum iron into the slurry feeding pipe 1 at multiple points to obtain first concentrated slurry, wherein the alkaline residue mass content in the first concentrated slurry is 35%; the mass ratio of the flocculant to the solid in the alkaline residue slurry is 5 mL: 1L of the compound.
S2, sending the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 31.6%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash, and preparing into mixed slurry with the solid mass content of 20%; the mass ratio of the fly ash to the solid in the concentrated slurry is 60 mL: 1L of the compound.
S3, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 0.5%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, wherein the water content of the alkaline residue filter cake is 43.8%, the chloride ion content is 0.8%, the sulfate ion content is 0.14%, and the filtrate is discharged to a second-stage high-efficiency thickener through a filtrate outlet header pipe.
< example 6>
The embodiment provides an impurity removal and purification process for alkaline residue in an ammonia-soda plant, which comprises the following steps:
s1, carrying out hydraulic flushing on the alkali residues deposited in the alkali residue field to form alkali residue slurry, mining the alkali residue slurry in the alkali residue field by using a cutter suction dredger, wherein the solid mass content of the alkali residue slurry is 20.0%, the water content is 90%, the chloride ion content is 10.1%, the sulfate ion content is 1.0%, the alkali residues deposited in the alkali residue field coexist in a solid state, a semi-solid state and a liquid state, the water content is 50% -90%, conveying the alkali residues to a first-stage high-efficiency thickener through a slurry feeding pipe 1, and adding polymeric ferric sulfate into the slurry feeding pipe 1 at multiple points to obtain first concentrated slurry, wherein the alkali residue mass content in the first concentrated slurry is 30.2%; the mass ratio of the flocculant to the solid in the alkaline residue slurry is 1 mL: 1L of the compound.
S2, sending the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 34.8%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash, and preparing into mixed slurry with the solid mass content of 18.3%; the mass ratio of the fly ash to the solid in the concentrated slurry is 100 mL: 1L of the compound.
S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content being reduced to below 0.5%, the sulfate ion content being reduced to below 0.2% and the water content being reduced to below 45%, wherein the water content of the alkaline residue filter cake is 43.5%, the chloride ion content is 0.7%, the sulfate ion content is 0.11%, and the filtrate is discharged to a second-stage high-efficiency thickener through a filtrate outlet header pipe.
While embodiments of the invention have been described above, it is not limited to the applications set forth in the description and the embodiments, which are fully applicable to various fields of endeavor for which the invention may be embodied with additional modifications as would be readily apparent to those skilled in the art, and the invention is therefore not limited to the details given herein and to the embodiments shown and described without departing from the generic concept as defined by the claims and their equivalents.
Claims (10)
1. An impurity removal and purification process for alkaline residue in an ammonia-soda plant is characterized by comprising the following steps:
s1, adopting a cutter suction dredger to collect alkaline residue slurry in an alkaline residue field, conveying the alkaline residue slurry to a first-level efficient thickener through a slurry feeding pipe, and adding a flocculating agent into the slurry feeding pipe at multiple points to obtain first concentrated slurry, wherein the mass content of alkaline residue in the first concentrated slurry is 25-35%;
s2, conveying the first concentrated slurry to a secondary efficient thickener to obtain second concentrated slurry, wherein the caustic sludge mass content in the second concentrated slurry is 25-35%;
s3, conveying the second concentrated slurry to a conditioning tank, adding fresh water and fly ash to prepare mixed slurry with the solid mass content of 10-20%;
and S4, feeding the mixed slurry into a diaphragm plate-and-frame filter press for full dehydration to obtain an alkaline residue filter cake with the chloride ion content reduced to below 0.5%, the sulfate ion content reduced to below 0.2% and the water content reduced to below 45%, and discharging the filtrate to a secondary high-efficiency thickener through a filtrate outlet header pipe.
2. An impurity removal and purification process for the caustic sludge of an ammonia-soda plant as claimed in claim 1, wherein the caustic sludge slurry in step S1 is formed by hydroexcavation of the caustic sludge deposited in the caustic sludge field, the solid mass content of the caustic sludge slurry is 8-20%, and the caustic sludge deposited in the caustic sludge field coexists in a solid state, a semi-solid state and a liquid state.
3. The process of claim 1, wherein the flocculating agent in step S1 is one or more selected from the group consisting of polyferric sulfate, polyaluminum sulfate, and polyaluminum ferric silicate.
4. The impurity removal and purification process of the alkaline residue in the ammonia-soda plant according to claim 1, wherein the mass ratio of the flocculant to the solid in the alkaline residue slurry in step S1 is (1-5 kg): 1 t.
5. The impurity removal and purification process of the alkaline residue in the ammonia-soda plant according to claim 1, wherein the flocculant is prepared into a flocculant solution with a mass content of 10% -30% in step S1, and the volume ratio of the flocculant solution to the alkaline residue slurry is (1-10 mL): 1L of the compound.
6. An impurity removal and purification process for alkaline residue in an ammonia-soda plant as claimed in claim 1, wherein the primary high-efficiency thickener and the secondary high-efficiency thickener comprise one of a high-efficiency deep cone thickener and an inclined plate thickener respectively.
7. The impurity removal and purification process of the alkaline residue in the ammonia-soda plant as claimed in claim 1, wherein the mass ratio of the fly ash to the solid in the second concentrated slurry is (20-200 kg): 1 t.
8. An impurity removal and purification process for the alkaline residue in the ammonia-soda plant as claimed in claim 1, wherein fresh water is added into the fly ash to prepare fly ash slurry with the mass content of 10% -20%, and the volume ratio of the fly ash slurry to the alkaline residue slurry is (20-100 mL): 1L of the compound.
9. The purification device for the purification process of the alkaline residue in the ammonia-soda plant according to any one of claims 1 to 8, comprising: the device comprises a twisting suction ship, a slurry feeding pipe, a primary high-efficiency thickener, a conditioning tank, a diaphragm plate and frame filter press and a secondary high-efficiency thickener, wherein one end of the slurry feeding pipe is communicated with the twisting suction ship, the other end of the slurry feeding pipe is communicated with the primary high-efficiency thickener, the primary high-efficiency thickener is communicated with the secondary high-efficiency thickener, the secondary high-efficiency thickener is communicated with the conditioning tank, the conditioning tank is communicated with the diaphragm plate and frame filter press, and the diaphragm plate and frame filter press discharges filtrate into the secondary high-efficiency thickener.
10. The purification device for the purification process of the alkali residues in the ammonia-alkali plant according to claim 9, wherein a plurality of adding holes are arranged on the pulp feeding pipe at intervals, each adding hole is vertically inserted into a steel pipe, the feeding end of each steel pipe is funnel-shaped, and the feeding end of each steel pipe corresponds to one opening of the flocculant adding pipe;
the pulp feeding pipe is perpendicular to the primary high-efficiency thickener and is connected with the central feeding cylinder.
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