CN1856455A - Reclaiming of organics with metal - Google Patents
Reclaiming of organics with metal Download PDFInfo
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- CN1856455A CN1856455A CNA2004800215987A CN200480021598A CN1856455A CN 1856455 A CN1856455 A CN 1856455A CN A2004800215987 A CNA2004800215987 A CN A2004800215987A CN 200480021598 A CN200480021598 A CN 200480021598A CN 1856455 A CN1856455 A CN 1856455A
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- Prior art keywords
- salt
- metal
- slurry
- product
- fertilizer
- Prior art date
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- 229910052751 metal Inorganic materials 0.000 title claims abstract description 21
- 239000002184 metal Substances 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 102
- 239000002002 slurry Substances 0.000 claims abstract description 64
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 60
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 56
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000003337 fertilizer Substances 0.000 claims abstract description 47
- 239000002253 acid Substances 0.000 claims abstract description 31
- 229910052742 iron Inorganic materials 0.000 claims abstract description 30
- 239000000203 mixture Substances 0.000 claims abstract description 28
- 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 claims abstract description 20
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims abstract description 20
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims abstract description 18
- 150000003839 salts Chemical class 0.000 claims abstract description 12
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 11
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims abstract description 9
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000012530 fluid Substances 0.000 claims abstract description 8
- 239000011790 ferrous sulphate Substances 0.000 claims abstract description 6
- 235000003891 ferrous sulphate Nutrition 0.000 claims abstract description 6
- 229910000358 iron sulfate Inorganic materials 0.000 claims abstract description 6
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims abstract description 6
- 150000003751 zinc Chemical class 0.000 claims abstract description 5
- 239000011787 zinc oxide Substances 0.000 claims abstract description 4
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims abstract description 4
- 229910000368 zinc sulfate Inorganic materials 0.000 claims abstract description 4
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- 239000000126 substance Substances 0.000 claims description 32
- 230000008569 process Effects 0.000 claims description 31
- 239000000428 dust Substances 0.000 claims description 21
- 239000007787 solid Substances 0.000 claims description 15
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 13
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- 238000005469 granulation Methods 0.000 claims description 9
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- 238000003860 storage Methods 0.000 claims description 8
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- 239000005864 Sulphur Substances 0.000 claims description 6
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 6
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 6
- 238000012423 maintenance Methods 0.000 claims description 6
- -1 sulphur compound Chemical class 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 5
- 238000005496 tempering Methods 0.000 claims description 5
- 239000004254 Ammonium phosphate Substances 0.000 claims description 4
- 229910000148 ammonium phosphate Inorganic materials 0.000 claims description 4
- 235000019289 ammonium phosphates Nutrition 0.000 claims description 4
- 230000007073 chemical hydrolysis Effects 0.000 claims description 4
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 abstract description 9
- 239000011701 zinc Substances 0.000 abstract description 9
- 229910052725 zinc Inorganic materials 0.000 abstract description 9
- 239000008187 granular material Substances 0.000 abstract description 4
- 239000011368 organic material Substances 0.000 abstract 4
- 159000000014 iron salts Chemical class 0.000 abstract 1
- 238000010186 staining Methods 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 62
- 239000000463 material Substances 0.000 description 43
- 239000000047 product Substances 0.000 description 38
- 229910021529 ammonia Inorganic materials 0.000 description 31
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 24
- 238000006243 chemical reaction Methods 0.000 description 23
- 239000000843 powder Substances 0.000 description 20
- 239000010815 organic waste Substances 0.000 description 19
- 239000002245 particle Substances 0.000 description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 12
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 12
- 239000003546 flue gas Substances 0.000 description 12
- 239000010801 sewage sludge Substances 0.000 description 12
- 239000010802 sludge Substances 0.000 description 12
- 239000003513 alkali Substances 0.000 description 10
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- 241000196324 Embryophyta Species 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000002585 base Substances 0.000 description 3
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- 150000007516 brønsted-lowry acids Chemical class 0.000 description 3
- 150000007528 brønsted-lowry bases Chemical class 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 230000001351 cycling effect Effects 0.000 description 3
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- 229940072033 potash Drugs 0.000 description 3
- 239000011591 potassium Substances 0.000 description 3
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 3
- 235000015320 potassium carbonate Nutrition 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
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- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- 239000004809 Teflon Substances 0.000 description 2
- 229920006362 Teflon® Polymers 0.000 description 2
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- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 241001672694 Citrus reticulata Species 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 241000270722 Crocodylidae Species 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
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- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 1
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- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical class [N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 description 1
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- 150000001413 amino acids Chemical class 0.000 description 1
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- 230000002349 favourable effect Effects 0.000 description 1
- RAQDACVRFCEPDA-UHFFFAOYSA-L ferrous carbonate Chemical compound [Fe+2].[O-]C([O-])=O RAQDACVRFCEPDA-UHFFFAOYSA-L 0.000 description 1
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- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 238000005246 galvanizing Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
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- 229910000398 iron phosphate Inorganic materials 0.000 description 1
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical group [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
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- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
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Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
Landscapes
- Fertilizers (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention is directed to methods for producing a granular nitrogen fertilizer from an organic material comprising adding a metallic salt to said organic material to form a slurry. Preferably the organic material comprises dewatered biosolids and contains water from a scrubber. Metallic salts that can be used comprise a salt of iron, zinc, or a mixture thereof. Preferred iron salts comprises ferric sulfate or ferric oxide, and preferred zinc salts comprises zinc sulfate or zinc oxide. Preferably, the metallic salt is mixed with an acid such as sulfuric acid to form an acidified metal salt. Slurry pH ranges from approximately 2-2.5. The acidified metal salt is added to the organic material in sufficient quantity to lower viscosity of the slurry such that the resulting fluid does not hinder fluid flow during operation. When the metallic salt comprises acidified ferric sulfate or ferrous sulfate, sufficient iron can be present to produce a fertilizer product with 0.1 weight percent to 10 weight percent iron sulfate calculated on a dry weight basis. The invention is also directed to fertilizer products made by the methods of the invention. Preferred products are granules and the metallic salt increases product hardness. Fertilizer granules preferably contain metal that is bioavailable to a plant when used as a fertilizer. Solubility of the metal of the product in water is enhanced, and the product is low staining.
Description
Quoting of related application
The application requires name to be called the U.S. Provisional Application 60/473 of " Organic Recycling with Metal Addition ", 197 and name be called the U.S. Provisional Application 60/473 of " Liquid Fertilizer Incorporating Biosolids andHigh Concentrations of Ammonia ", 198 right of priority, their full content all is combined in this by reference.
Background of invention
1. invention field
The present invention relates to organic substance is transformed into system, the apparatus and method of fertilizer.More specifically, the present invention relates to before making fertilizer, in organic substance, add ferric sulfate or other metal-salt by organic substance.
2. background is described
The disposal of sewage sludge is a great worldwide problem.The method of disposing at present sewage sludge comprises: burn, directly the soil or the ocean utilizes, with the mud heating and dry with sterilization apply it to the soil then, it is deposited in the landfill yard or with the rotary granulator of standard with the mud granulation; wherein the thermal source (for example, the fuel of buying by burning) by the outside provides heating and dry.Though some in these methods have obtained fertilizer, this fertilizer has low relatively decomposition for their plant nutrition value.
The method that the plant nutrition of expression fertilizer is worth comprises: the NPK value of identification fertilizer, and wherein N relates to the amount of nitrogen, and the amount that P relates to phosphorus (is expressed as P
2O
5) and the K amount that relates to potassium (be expressed as K
2O).Therefore, as United States Patent (USP) 3,050,383 are reported, the sewage sludge with 2.5/2.5/0 value contains 2.5% nitrogen, 2.5% by P
2O
5The phosphorus and 0% of meter is pressed K
2The potassium of O meter.Unless carry out different indications by use, the per-cent that all percent value here all are based on weight (that is, w/w).
Luckily, the method that has the nutritive value that improves low relatively decomposition organic waste materials.For example, in the described in the above Wilson patent (its content is combined in this by reference and intactly), a kind of method is disclosed, this method is used for the acid of controlled quatity such as sulfuric acid, phosphoric acid (or the phosphorus compound of equivalent, its intensity is expressed as phosphoric acid) or they mixture and water containing ammonia such as ammoniacal liquor or contain the ammonia nitrogen salts solution and handle exsiccant animal muck and sewage sludge, and the reactive material that obtains of rolling has the fertiliser granulates that plant nutrition enriching or that improve is worth with generation.
(for example, United States Patent (USP) 4,743 also to have described other method of using acid, alkali or their mixture to improve low relatively decomposition organic waste materials, 287, the open T955 of U.S.'s defence, 002, Norton etc. (on February 1st, 1977), United States Patent (USP) 5,466,273, United States Patent (USP) 5,125,951, United States Patent (USP) 5,118, and 337, United States Patent (USP) 5,393,317 and United States Patent (USP) 5,422,015.
Be known in the art tubular reactor and be used to make ammonium salt (for example, United States Patent (USP) 6,117,406, United States Patent (USP) 2,902,342, United States Patent (USP) 2,755,176 and United States Patent (USP) 2,568,901, the content of these patents is combined in this by reference).In tubular reactor, carry out thermopositive reaction by alkali with sour reaction in reactor tube.European patent discloses 770, and 586A1 also discloses and tubular reactor can be used for handling the low relatively organic waste materials that decomposes.This European patent has openly been described a kind of by tubular reactor being introduced in described organic waste materials, ammonia and acid, carry out thermopositive reaction, separate steam from mud, further being handled the method that mud is handled this organic waste materials then prevailingly.
The assembly relevant with the tubular reactor typical case is the pre-neutralization device.Typically pre-neutralization device and tubular reactor are united use, before being introduced into reactor in acid its part is neutralized.But the use of pre-neutralization device has various shortcomings, comprises the accurate control that is difficult to obtain flow velocity.In addition, relevant with using the pre-neutralization device operation and cost of equipment are usually expressed as significant expense.
The reactor that is similar to tubular reactor is a pipe cross reactor.Similarly, pipe cross reactor allows thermopositive reaction to take place, and will be used in the method introducing with one or both different acid solutions of alkali reaction but typically be included in, with thorough mix reagent.This is a key character of pipe cross reactor, because it has eliminated the needs of pre-neutralization device.In the first step of pipe cross reactor, with alkali and/or washer water and the pre-mixing of organic substance solution.In second step, form pipe cross reactor with maximum two sour imports, described sour import is so set up, and makes acid solution is introduced perpendicular to pipe cross reactor, as the stream of substantial reverse.Vertically enter with reverse direction flow and make acid mixing fully in reactor, thereby eliminated the needs of peripheral equipment such as pre-neutralization device.
Pipe cross reactor is well-known, and be used in the past (for example make granular NPKS fertilizer by liquid chemical, Energy Efficient Fertilizer Production with thePipe-Cross Reactor (U.S.Dept.of Energy, 1982) (a pipe-cross reactor fit intothe granulator drum of a conventional ammoniation-granulation system); Achom etc., and " Optimizing Use of Energy in the Production of GranularAmmonium Phosphate Fertilizer " (1982 Technical Conference of ISMA, Pallini Beach, Greece); British Sulfur Corp.Ltd., " TVA modifies its pipereactor for increased versatility ", Phosphorus ﹠amp; Potassium, No.90,25-30 page or leaf (1977); Achorn etc., " Efficient Use of Energy in Production of Granular andFluid Ammonium Phosphate Fertilizers " (1982 Fertilization Association ofIndia Seminar, New Dehli, India); Salladay etc., " Commercialization of the TVAPipe-Cross Reactor in Regional NPKS and DAP Granulation Plants in theUnited States " (1980 Fertilization Association of India Seminar, New Dehli, India); United States Patent (USP) 4,619,684; United States Patent (USP) 4,377,406; United States Patent (USP) 4,134,750; The open T969 of U.S.'s defence of Norton etc., 002 (on April 4th, 1978); With Salladay etc., and " Status of NPKS Ammoniation-Granulation Plants and TVA Pipe-CrossReactor " (1980 Fertilizer Industry Round Table, Atlanta, GA, US)).Recently, pipe cross reactor successfully has been used for improving relatively low plant nutrition of decomposing organic waste materials and has been worth (for example, United States Patent (USP) 5,984,992 and 6,159,263, the full content of these two pieces of patents all is combined in this by reference).
A potential shortcoming with reactor such as pipe cross reactor or the low relatively decomposition organic waste materials of tubular reactor heat release processing is that the discharging noxious odor may in treating processes.The pipe cross reactor that use is used to handle this refuse helps to reduce typically relevant with its processing smell.But, have needs for providing this potential smell to be eliminated or reducing the bigger assurance that surpasses present emission level at least.
In addition, for improving sludge treatment, aspect two of capital outlay and process costs, all there is the expectation that continues.
In the art, need under the condition that does not have the noxious odor discharging basically, the low relatively organic waste materials that decomposes be treated as the simple and efficient relatively method that improves plant nutrition value composition.Preferably, this method can be made the product of classification and moulding, to be sold by commercial dealer.
Summary of the invention
The present invention has overcome and present strategy and relevant problem and the shortcoming of design, and the novel method by organic substance manufacturing fertilizer is provided, described organic substance such as biosolids but be not limited to biosolids.The present invention also provides the fertilizer of being made by method of the present invention.
One embodiment of the invention relate to the method for being made granular nitrogenous fertilizer by organic substance, and this method comprises that the adding metal-salt is to form slurry in described organic substance.Preferably, organic substance comprises the dehydration biosolids and contains water from washer.Operable metal-salt comprises molysite, zinc salt or their mixture.Preferred molysite comprises ferric sulfate or ferric oxide, and preferred zinc salt comprises zinc sulfate or zinc oxide.Preferably, metal-salt is mixed as sulfuric acid with acid, to generate acidified metal salt.Slurry pH scope is about 2-2.5.Described acidified metal salt is added in the described organic substance with the amount that is enough to reduce described slurry viscosity, and the fluid that obtains does not hinder fluid flow in operating process.When described metal-salt comprises acidifying ferric sulfate or ferrous sulfate, can exist enough iron to have fertilizer product by dry weight 0.1 weight % to 10 weight % ferric sulfate in preparation.When being added to sulfuric acid in the organic substance, preferably it is added before arriving tempering tank and with the speed of about 1.75% total feed rate, obtain 3.0 to 3.5 pH scope.
Preferably, slurry is pumped in the shear-mixed groove that contains the high-shear gyratory shaker, described stirrer is to be enough to produce the speed rotation of high shear force.Make slurry by described shear-mixed groove to maintenance that contains stirrer or compensating groove.Described stirrer can provide about 2 hours or above storage for slurry.Can operate maintenance or compensating groove, be 3.0 to 4.0 to keep pH, and wherein solids content is 15% to 28% solid.Metal-salt can combine with one or more element chemistries of slurry.When using molysite, iron can combine with ammonium sulfate or the ammonium phosphate in being present in described slurry.This can improve granulation and form, and reduces sulphur compound and smell in operating process and dust formation in described slurry.
Preferably, metal-salt has caused the chemical hydrolysis of the organic molecule in described slurry.This can displace organic substance with sulphur compound, thereby reduces the odor source in the fertilizer product that obtains.
Preferably, metal-salt is added in the organic substance in pipe cross reactor or tubular reactor.Metal-salt has improved the reaction kinetics of described pipe cross reactor and has reduced the viscosity of slurry, makes that the operation of pipe cross reactor is more controlled than the situation that does not have metal-salt.
Another embodiment of the invention relates to the fertilizer product of being made by method of the present invention.Preferred product is a particle, and metal-salt has improved the hardness of product.The pulverizing weight of product can be greater than 6 pounds, or are preferably greater than 7 pounds.Preferred fertiliser granulates contains metal, but described metal is a biological utilisation for plant as fertilizer the time.The solubleness of the metal of described product in water is improved, and this product is oligosaprobic.
Other embodiment of the present invention and advantage are partly listed in the following description, and part can to describe thus be significantly, or can be instructed by practice of the present invention.
Description of drawings
The process flow sheet of Fig. 1 one embodiment of the invention.
The imitation figure of Fig. 2 pipe cross reactor.
The part of the pipe cross reactor of Fig. 3 in rotation ammoniator-tablets press cuts, skeleton view.
The imitation end view of the rotating bed of the material in Fig. 4 tablets press.
The side-view of the orifice plate that Fig. 5 pipe cross reactor is utilized.
The artwork of an embodiment of Fig. 6 pre-treatment slurry.
Invention is described
So the place is specialized and is broadly described, the present invention relates to handle the system and the method for organic substance.More specifically, system and the method that the present invention relates to handle mud and mud is transformed into fertilizer.
As shown in Figure 1, the method that is worth of a kind of plant nutrition that is used to improve organic waste materials generally includes: organic waste materials is mixed with water 10.Be used for organic waste materials and a kind of preferred method of water blended are described in Fig. 6.Preferably, this method comprises organic waste and fluid (as water but be not limited to water) is mixed with metal-salt (preferred molysite).The water that uses in the preparation slurry can comprise the washer water from washer 38 described below ideally, and it can comprise spent acid.This slurry mixes under enough concentration and denseness, makes preferably to handle organic waste materials as quickly as possible, but can not block or stop up reactor in operating process.A kind of preferred reactor is a pipe cross reactor 12, but can alternatively use tubular reactor, even unites use with pipe cross reactor in an individual system.Specific slurry concentration and denseness can depend on the size of the particulate matter material that contains and the size and the length of quantity and reactor parts to a certain extent in specific organic waste materials.But when being sent to pipe cross reactor, it is about 5% that the solids content of slurry is at least usually, and can be up to about 35%.Preferably, the solids content of slurry is about 10% to 30%, and is more preferably about 14% to 28%, and more preferably about again 15% to 22%.
As shown in Figure 1, slurry is pumped to the pipe cross reactor 12 that is used for thermopositive reaction from steel basin 10, described pipe cross reactor 12 contains alkali such as ammonia and one or more acid as sulfuric acid, phosphoric acid and their mixture, is with or without extra water, melts body with formation.
Determine the amount of the bronsted lowry acids and bases bronsted lowry that in exothermic process, uses by those skilled in the art.But,,, use about 1 mole sulfuric acid or two moles of phosphorus compounds by phosphoric acid for per two moles ammonia as the guidance of neutralization of ammonia.As for concentration of phosphoric acid, the typical mol ratio of N in pipe cross reactor: P is 0.4: 1 to 0.7: 1, be preferably 0.55 to 0.65: 1, as for vitriolic concentration, the typical mol ratio of N in pipe cross reactor: S is 0.5: 1 to 0.8: 1, is preferably 0.65: 1 to 0.72: 1.The molar weight of nitrogen not only should be considered the ammonia amount that adds, also should consider the typical amount of the ammonia nitrogen that contains in specific organic waste materials.
Operable other acid of the present invention comprises nitric acid, acetate, citric acid and their mixture, all these is that those skilled in the art are known (for example, nitric acid and ammoniate, they can generate the ammonium nitrate of blast in the presence of organic substance).Select any acid or multiple acid, the intensity of one of acid of using in method will preferably be equivalent to 90% sulfuric acid (for example, 93 to 100% sulfuric acid).
As shown in Figure 2, preferred pipe cross reactor 12 is equipped with two cross tubes 26,28, to accept sulfuric acid (under about speed of 17.2 to 25.8gpm) and phosphoric acid (under about speed of 5.2 to 7.8gpm).The 3rd pipe 30 is incorporated into ammonia or near the center of reactor.The length of pipe 30 is desirably at least 20 to 30 inches, to guarantee sufficient mixing.The 3rd cross tube 32 is incorporated into slurry and extra water in the mixing section.Between the 3rd cross tube 32 and first, second root cross tube 26 and 28 is orifice plate 33, and it is used to turbulent flow is introduced in the slurry flow, thereby guarantees bigger mixing.
The diameter that is used for typical pipe cross reactor of the present invention is about 3 to 10 inches, about 7 to about 15 feet long, and preferred with rust steel pad or TEFLON
TMLining is terminated at for example 2 to 8 inches delivery pipe (or slit of equal sectional area).Delivery pipe preferably drains in the rotary drum granulator 14 of standard, and is preferably made by steel pipe (for example, HASTELLOY C-276 or 316L stainless steel (wherein HASTELLOY C or B are used for reaction tubes)).In pipe cross reactor, can also use TEFLON
TM, the pottery or other applied corrosion resistant lining.The preferred temperature that keeps is lower than 204 ℃ (400 ).
As shown in Figure 5, orifice plate 33 comprises the plate that is formed by the material that is similar to pipe cross reactor 12, and comprises hole 35 or aperture, and its diameter is littler than the diameter of pipe cross reactor 12.Therefore, for example the pipe cross reactor of (6) inch diameter has the orifice plate 33 in hole 35 with employing, and the diameter that described hole 33 demonstrates is less than several inches, for example several inches.When determining hole 35 big or small, can consider various parameters, comprise the solids content of the flow velocity and the slurry of slurry, bronsted lowry acids and bases bronsted lowry.Therefore, for given pipe cross reactor 12,, then can change the size in hole 35 if change any processing parameter.
Although Figure 5 shows that the use of circular orifice, be surprisingly found out that adding projection in order to improve two pipe cross reactor upstream turbulent flows provides bigger heat recuperation usually.In other embodiments, by using with respect to flow series connection or parallel projection such as bump, a plurality of bump, one or more wire rod, input gas under pressure such as air use sonic vibrator or at the vibration wall of this position, and turbulization.For example, can use 2,3,4,5,6,7,8 or more a plurality of equally spaced bump come turbulization, each bump by for example 0.02,0.05,0.1,0.2 or 0.3 times at the diameter of this point and outstanding entering towards tube chamber intermediary space.In one embodiment, bump is annular reinforcement, and it forms converging duct in pipe.Can also use sonic vibrator, for example the sonic vibrator that provides by Advanced Sonics.Shown in Fig. 2 and 5, converging duct is not necessary for circular, and can be another kind of cross-sectional shape, as avette, square or irregular shape.Avette part is desired, particularly has the avette part of the narrow and small end of pointing to cross tube, makes that the avette axle of length strides across the line that connects two cross tube openings and extends.In another embodiment, avette minor axis strides across the line that connects two cross tube openings and extends.Have turbulent flow that the oval shape of long coupling axle provides with from the more closely knit coupling of the inlet flow of vertical cross reactor, and when the vertical cross tube reactor that uses as shown in Figure 2, be to expect especially.
The optimal placement of one or more projections is 0.1 to 3 flow diameters of cross reactor outlet mean place (that is, cross reactor outlet average, its flow length that can stagger downwards) upstream in many embodiments.More preferably, projection is between 0.3 to 1.5 diameter of cross tube reactor front.Optimal placement will change according to flow velocity.For very high flow velocity, one or more projections will be set to farther, or the degree that projection enters runner should be restricted.This embodiment can be undertaken by adjustable annular collar or adjustable bump, and described adjustable annular collar or adjustable bump provide the runner that is controlled at outer distance and projection to enter the ability of degree.For example, can regulate annular collar with suitable openings of sizes, and annular collar can be placed in alternate positions.If use, a plurality of sonic vibrators can be placed in different positions, and switch individually, to adapt to the viscosity of (vibration of more close cross tube) of slowing down or (more distant positions) flow velocity and/or reduction faster.
For given viscosity and flow velocity, can be with the adjusting optimizing of cross tube reactor itself.In many embodiments, advantageously, the cross reactor tube just in time toward each other, as shown in Figure 2.When adding can be compared the fluid of viscosity under comparable flow velocity, this layout was an ideal.Using a plurality of (3 or 4 or more a plurality of) cross tube also is ideal.For example, if viscosity is enough low, can use four paths (four vertical tube) of two kinds of materials of control, every kind of material is by two reverse sides.A plurality of cross reactor tubes can be switched, to adapt to the change of viscosity and/or flow velocity.For example, by using one or more cross Reactor inlet, described opening is away from (more downstream) one or more projections, and can open and close, can favourable more low-viscosity material or the system of high flow rate more.Mobile by changing, and/or the kind of mud material and/or reagent, monitor heat recuperation by the temperature of measuring one or more some place, downstream then, can make other combination optimizing at daily timing.By adjustable one or more projection is provided, and/or cross tube arranges and/or flow velocity, can obtain best heat recuperation.
Another embodiment provides a kind of automatic system again, its certain point in the cross tube reactor downstream is constantly monitored the temperature of compounding substances, and regulates the switching of the layout of projection, the flow velocity of mud, the flow velocity of alkali, the flow velocity that adds entry, one or more sour flow velocitys and cross tube reactor outlet for the effect of the best.In an ideal embodiment, regulate the flow velocity of alkali up or down, and/or the flow velocity of dilution water, and/or the flow velocity of acid, and/or the flow velocity of second kind of acid, and/or the flow velocity of mud, to obtain higher temperature.In another embodiment, between two or more cross tubes, select switch, to obtain better temperature.In another embodiment again, during some heat transmission that controllably will discharge feed back and become a mandarin, think that sufficient mixing obtains better viscosity.According to the heat that reclaims, or according to the back-pressure of another kind of monitored parameters such as one or more sludge pumps or the back-pressure of measuring at pipe cross reactor rule place, Controlling System can be regulated the heat transmission up or down.
Do not wish that this embodiment of the present invention is bound by any theory, by near in orifice plate 33 downstreams and common turbulization zone first and second cross tubes 26 and 28, projection such as orifice plate or other mechanism or device can bigger ground mixed slurry.The increase turbulent flow of the Chan Shenging generation that improved heat in many cases is as measured by higher melt body temperature.This temperature can also be measured as 1 or 2 pipe diameter place that last root cross tube downstream is farther in last root cross tube place or downstream of adding reagent.The use of having observed orifice plate has the effect that improves heat recuperation, improves up to about 30% than the pipe cross reactor that does not similarly have orifice plate.If desired, orifice plate 33 can be changed the another kind of orifice plate for the hole 35 with different diameter.
With reference to figure 2, the speed of ammonia with about 4.3gpm is introduced in the representative system described herein.Organic waste materials (for example, sewage sludge) and water are merged with about 30 to about 40gpm slurry speed.Pipe cross reactor shown here is typically operated under 15 to 60psig gauge pressure.
Heat is melted body and is drained into the tablets press 14 from pipe cross reactor 12, simultaneously water it from flow into tablets press 14 time from reactor product flash distillation come out.Produce steam by the thermopositive reaction of in pipe cross reactor 12, carrying out.
A kind of preferred tablets press (for example, ammoniator-tablets press) is depicted in Fig. 3 and 4, is a kind of tablets press of 2 to 4 rice diameter rotary drums, and its length is about 5 to about 9 meters.As shown in Figure 3, with pipe cross reactor 12 vertically orients, and comprised that before entering tablets press 14 quantity is 90 transition or elbow.Position shown in the pipe cross reactor 12 is preferred, because it provides bigger mixing capacity.But, can reach satisfied result (for example, United States Patent (USP) 5,984,992 and 6,159,263) by pipe cross reactor 12 without any transition or elbow, horizontal location.
In described method, tablets press 14 comprises the ammonia sparger 20 that operationally is arranged in tablets press 14, is used for ammonia is added to melting body, to finish the acid-base reaction of finished product.To melt body in tablets press 14, rolling on the round-robin particulate, and, thereby make granular particle grow to needed size with the formation granular particle.Then, as shown in Figure 1, these granular particle are fed the sufficiently long time in the spin drier 16,, improve the fertilizer that plant nutrition is worth thereby form to have to reduce their moisture content.Also the steam that forms between the reaction period with slurry and bronsted lowry acids and bases bronsted lowry (for example, the steam that flashes off) is collected and is delivered in the spin drier 16, is used to improve the dew point of steam, with not condensation in shop equipment.
With United States Patent (USP) 5,984,992 and 6,159,263 method is compared, and it is a kind of alternative methods that such steam is directly fed in the moisture eliminator 16.The formerly method relevant with pipe cross reactor typically separated granular particle and steam before the drying granular particle, was used for independently handling.The method of describing has been eliminated the needs of extra separation of particles equipment and processing air at present, causes simpler and more efficient methods at last.
A kind of to be used for preferred moisture eliminator of the present invention be 2 to 4 rice diameter rotary drum driers, and its length is about 17 to about 33 meters, and to add thermal capacity be 30 to 7,000 ten thousand BTU/ hours, at discharge end the agglomerate pulverizer arranged.
This method also comprises will make the exsiccant granular particle pass through particle sorting apparatus, as sieve 18, and the exsiccant saccharoid is separated into fine powder, product and excessive material.Excessive material size is reduced, merge back in the technology as fine powder.Fine powder is returned tablets press 14 (with potash or any micro-nutrient of required check analysis requirement), be used for integrating with technology.
In the process of carrying out, the flue gas that can contain ammonia, particulate and be higher than the water vapor of its dew point is collected from moisture eliminator 16, and by separation of particles equipment such as tornado dust collector 34.Tornado dust collector 34 are removed the part particulate from air, and with these particulates (for example, dust) and fine powder with grind material and reclaim.The flue gas that obtains leaves tornado dust collector 34, and handles by extra separation of particles equipment such as bag filter 36.Bag filter is used for removing the particulate of additional quantity, particularly has the particulate littler than the particle size of removing by tornado dust collector 34.Similarly, the particulate that will remove from bag filter 36 and fine powder and grind material and reclaim are used for tablets press 14.
Leave the flue gas of bag filter 36 and then handle by washer 38, described washer 38 is as Venturi scrubber or bed of packings washer, and it comprises the water sepn chamber that is used to collect ammonia flue gas and little powder dust particle.The present invention uses low pH water in washer 38, to collect the unreacted ammonia steam of escaping from tablets press 14.In one embodiment, in washer 38, add a spot of sulfuric acid or phosphoric acid, to keep being suitable for the low pH (for example, 2 to 3) of ammonia steaming.
This method comprises that also the air that will come out carries out oxidation, for example carries out oxidation in regenerative heat oxidizer (RTO) 40 from washer.RTO 40 is used for destroying volatile organic compounds (VOC) and other hydrocarbon gas pollutent, otherwise they will be released in the atmosphere.RTO 40 destroys VOC and hydro carbons flue gas by the high-temperature thermal oxidation method, and VOC and flue gas are transformed into carbonic acid gas and water vapor.The oxidation of air also is used for eliminating basically any noxious odor, otherwise they will enter to atmosphere.The energy that discharges from oxidising process can circulate, to reduce process cost.
Air is extracted out from RTO 40, and entered in the atmosphere by chimney 42.This method can advantageously comprise: before alkali (for example, ammonia) is introduced into pipe cross reactor 12 and/or is introduced in the tablets press 14 by sparger 20, use the heat from chimney 42 discharges to come pre-thermokalite.
For described process, airy comprises on the other hand from sieving collects air 18.This process is paid close attention to two points, and these two points comprise the removal of particulate and the circulation of particulate and air.First option comprises by 34 pairs of air of tornado dust collector to be handled, and particulate and air cycle are got back in the tablets press 14.Second option comprises and utilizes tornado dust collector 34, but also comprises by 36 pairs of air of bag filter and handling, and regathers particulate and is used for circulating at tablets press.The air that leaves bag filter 36 is sent to moisture eliminator 16 rather than tablets press 14.
The others that are used for ventilation system of the present invention preferably include fan, are used for air was moved into and shifts out from the above-described different treatment stage.The volume of air that moves is determined by the amount (being higher than dew point) of the moisture that will remove and the fusing point or the dissociation temperature of fertilizer product.
NPK fertilizer preferably includes micro-nutrient iron and zinc.An embodiment preferred, will be used to keep the low pH of washer water from the spent acid of hot dip process zinc or steel pickling process.These spent acid normally contain the sulfuric acid of 5 to 10% intensity of 3 to 8% iron.Zinc-plated spent acid contains and iron 3 to 8% zinc together.Be fed to the mud slurry tank with iron and zinc and from the water that is loaded with ammonia of washing, and reach pipe cross reactor, be used for being combined in last NPK fertilizer as iron and zinc micro-nutrient.Under useless vitriolic situation, sulphur also in the fertilizer that obtains as nutrient generate ammonium sulfate because it reacts in pipe cross reactor.
Other micro-nutrient or other composition can be combined in the fertilizer that obtains by with weigh-feeder they being added in the fine powder cycling stream as drying solid.Micro-nutrient or other composition (for example preferably include lime, rhombspar, calcite, hydro biotite, gypsum, phosphoric acid salt, rock phosphate or ammonium phosphate), potash, urea, soil clay, calcium peroxide, ammonium nitrate, vermiculite, humic acids and trace mineral, as iron, manganese, magnesium, boron, copper and zinc, and their combination.
Although the present invention has been described in the processing for city sewage and sludge especially, but, the inventive method can also be used for improving other low relatively plant nutrition of decomposing organic waste materials is worth, described other low relatively organic waste materials such as poultry manure, food-processing refuse, refuse, pig manure mud, environment or industrial biomaterial of decomposing from papermaking, their mixture, etc.Under these circumstances, with the specific low relatively sewage sludge that decomposes in the organic waste materials alternative method, and correspondingly regulate processing parameter.
Provide the following examples to be used to illustrate embodiment of the present invention, but not will be understood that embodiment limits the scope of the present invention.
Embodiment
Embodiment 1
In steel basin, the sewage sludge of 6700 kilograms/hour (7.4 tons/hour) is mixed with the washer water of 37 liters/minute (10 gallon per minute (gpm)), form slurry.This slurry has such denseness (solids content changes) between 10% and 27%, make it to be pumped to outfit with positive-displacement pump or other suitable pump and receive in the pipe cross reactor of ammonia, sulfuric acid, phosphoric acid, sewage sludge and water.The diameter of pipe cross reactor is about 4 inches, and is 40 feet long.Pipe cross reactor is terminated at rotary drum granulator.The diameter of rotary drum granulator is that 6 feet and length are 20 feet.
Slurry is added in the pipe cross reactor, and with the phosphoric acid (54%P of the ammonia of 8.6gpm 99.5%, the sulfuric acid of 8.6gpm (93%) and 2.6gpm
2O
5) reaction.The moisture that the temperature of pipe cross reactor (because the thermopositive reaction between acid and the alkali) is used in the mud is maintained at about 149 ℃ (300 ).This temperature (being higher than the minimum bactericidal temperature) has other pathogenic agent of killing salmonella, intestinal bacteria and can finding in slurry effect.This temperature also has the effect of this material being carried out deodorization to a certain degree.
With obtain from the Repone K (60%K that melts body and 2000 pounds of addings with pipe cross reactor
2O) spray together on the circulation bed of fine powder, the water that in melting body, contains simultaneously as steam flash distillation come out.The ammonia sparger is provided in tablets press,, is used to finish reaction and particulate and finally hardens so that a spot of ammonia is added in the granulation mixture.
Pipe cross reactor with a kind of like this method operation merges 20% about 14.8 tons/hour solid sewage sludge with 10 tons/hour throughput rates.
Particulate matter at about 93 ℃ (200 ) down and come out to enter in the spin drier under about 5 to 15% moisture contents from tablets press.The diameter of spin drier is about 2 meters, and length is about 20 meters.Its thermal capacity that adds is 3,000 ten thousand BTU/ hours, and unites in discharge end agglomerate pulverizer or agglomerate crusher are arranged.Will the moisture in material be reduced to and be lower than 3% by the hot forced ventilation in moisture eliminator.
Making the material that comes out from spin drier pass the agglomerate pulverizer is reduced to less than 1 inch with the size with excessive material.
Sieve is used for separating substances become (a) fine powder, (b) product and (c) excessive material.Fine powder is back in the tablets press.Product is by 2 rice diameters, 20 meters long water coolers, then to storing, makes excessive material by masher and reduce to become fine powder simultaneously, is used for tablets press and reclaims.In cycling stream, require the fines/ton product of about 2 tons (1800kg).
The flue gas that will contain steam, ammonia and particulate from tablets press is by collecting the inner negative pressure that keeps of tablets press with fan, thereby flue gas is drawn to spin drier, to reduce its moisture content.Under the temperature and 100% relative humidity of 92 ℃ (198 ), air speed with 20,000 cubic feet/min (cfm) from tablets press is extracted out.This approximates the water of conveying 34,200 Pounds Per Hours (lbs/hr) and the dry air of 296 ppm (lbs/min).
The air of rotatable moisture eliminator of spinning is in the future guided tornado dust collector, bag filter into, is washer then.70, under the speed of 000cfm, 45% relative humidity, air is extracted out from moisture eliminator.The dry-bulb temperature that leaves the air of moisture eliminator is that about 93 ℃ (200 ) and wet-bulb temperature are about 74 ℃ (165 ).This approximates carries 56, the water of 100lbs/hr and 2, the dry air of 711lbs/min.The air that enters washer is washed with low pH water (by adding the water that reduces pH from the spent acid of hot-dip galvanizing technique).If can not obtain zinc-plated acid, can control pH with phosphoric acid or sulfuric acid.Low pH water is collected in ammonia steam and the powder dust particle that exists in the flue gas.
With 67, the speed of 100cfm, under the temperature of 165 and under the relative humidity 100% will be guided the regenerative heat oxidizer into from the air of washer.Then, under the temperature of 93 ℃ (200 ), oxidation air extracted out from the regenerative heat oxidizer and by about 100 (100) feet high smoke stack emissions.
Keep the equipment negative pressure by fan, the air that is loaded with dust is collected from masher and sieve.This air traction by cyclone system, is removed about 97% dust.From cyclonic separator, this air returns rotary pelleting machine and dust is added in the fine powder of recovery.
The NPK value of the fertilizer that obtains is 12-3-6 (12% a nitrogen, 3% phosphoric acid salt and 6% potash).It is still uniform, and has the suitable size for the standard application equipment.
Embodiment 2
In tubular reactor rather than pipe cross reactor, repeat the method for embodiment 1.In steel basin, the sewage sludge of 6700 kilograms/hour (7.4 tons/hour) is mixed with the washer water of 37 liters/minute (10 gallon per minute (gpm)), form slurry.This slurry has such denseness, makes it to be pumped to outfit with positive-displacement pump or other suitable pump and receives in the tubular reactor of ammonia, sulfuric acid, phosphoric acid, sewage sludge and water.The diameter of tubular reactor is preferably about 1.5 to 30cm, and length is 2 to 10 meters, preferred 5 to 8 meters.Tubular reactor is terminated at rotary drum granulator.The diameter of rotary drum granulator is that 6 feet and length are 20 feet.
Slurry is added in the reactor, and with the ammonia of 8.6gpm 99.5%, the sulfuric acid (93%) that contains 8.6gpm and the phosphoric acid (54%P of 2.6gpm
2O
5) acid solution reaction.The moisture that the temperature of reactor (because the thermopositive reaction between acid solution and the alkali) is used in the mud is maintained at about 149 ℃ (300 ).
With obtain from the Repone K (60%K that melts body and 2000 pounds of addings with reactor
2O) spray together on the circulation bed of fine powder, the water that in melting body, contains simultaneously as steam flash distillation come out.The ammonia sparger is provided in tablets press,, is used to finish reaction and particulate and finally hardens so that a spot of ammonia is added in the granulation mixture.
Particulate matter comes out to enter in the spin drier under moisture content condition approximately from tablets press.The diameter of spin drier is about 2 meters, and length is about 20 meters.Its thermal capacity that adds is 3,000 ten thousand BTU/ hours, and unites in discharge end agglomerate pulverizer or agglomerate crusher are arranged.Will the moisture in material be reduced to and be lower than 3% by the hot forced ventilation in moisture eliminator.
Making the material that comes out from spin drier pass the agglomerate pulverizer is reduced to less than 1 inch with the size with excessive material.
Sieve is used for separating substances become (a) fine powder, (b) product and (c) excessive material.Fine powder is back in the tablets press.Product is by 2 rice diameters, 20 meters long water coolers, then to storing, makes excessive material by masher and reduce to become fine powder simultaneously, is used for tablets press and reclaims.In cycling stream, require the fines/ton product of about 2 tons (1800kg).
The flue gas that will contain steam, ammonia and particulate from tablets press is by collecting the inner negative pressure that keeps of tablets press with fan, thereby flue gas is drawn to spin drier, to reduce its moisture content.Under the temperature and 100% relative humidity of 92 ℃ (198 ), air speed with 20,000 cubic feet/min (cfm) from tablets press is extracted out.This approximates the water of conveying 34,200 Pounds Per Hours (lbs/hr) and the dry air of 296 ppm (lbs/min).
The air of rotatable moisture eliminator of spinning is in the future guided tornado dust collector, bag filter into, is washer then.With 70, the speed of 000cfm, under 45% relative humidity is extracted air out from moisture eliminator.The dry-bulb temperature that leaves the air of moisture eliminator is that 93 ℃ (200 ) and wet-bulb temperature are 74 ℃ (165 ).This approximates carries 56, the water of 100lbs/hr and 2, the dry air of 711lbs/min.The air that enters washer is washed with low pH water.Low pH water is collected ammonia and the powder dust particle that exists in the flue gas.
With 67, the speed of 100cfm, under the temperature of (165 ) and under the relative humidity 100% will be guided the regenerative heat oxidizer into from the air of washer.Then, under the temperature of 93 ℃ (200 ), oxidation air extracted out from the regenerative heat oxidizer and by about 100 feet high smoke stack emissions.
Keep the equipment negative pressure by fan, the air that is loaded with dust is collected from masher and sieve.This air traction by cyclone system, is removed about 97% dust.From cyclonic separator, this air returns rotary pelleting machine and dust is added in the fine powder of recovery.Determine that the fertilizer that obtains has the NPK value.
Embodiment 3
Figure 6 shows that a kind of preferred method that before biosolids is transformed into fertilizer, prepares and handle.
In Fig. 6, urban biology solid 620 is formulated in 625 cubic yards the case.Preferably these chests are placed on the dummy car of suitable design, and are transported to the sludge treatment district.Open chest, and discharging is to hopper 622.It is about 47 cubic yards that the minimum of hopper 622 is preserved volume.The maximum volume of hopper 622 is stipulated by factory available space and overall in kind the arrangement.Hopper 622 preferably is made of in order to avoid owing to the wet environment in this district corrodes stainless steel.The big unlimited fire grate of preferred installation in hopper is to catch any big tramp material that may be present in the mud case.Preferably, the opening of this grid is about 1 ' x1 '.
Mud 620 enters into the bottom of hopper 622 through grid.In the bottom of hopper 622, usage level duplex screw rod 624.The duplex screw rod begins mud 620 is delivered to transferpump 626 from hopper 622.The quantity of screw rod, size and arrangement are by the geometrical shape regulation of hopper 622.In one embodiment, use 4 screw rods, with the feeding rate of control mud 620 in the alternative mode.Can use various screw rods.Preferably come drive screw by the direct drive gear electric motor of under the speed of the mud 620 that is enough to provide institute's required amount, operating for technology.Can by the operation of screw rod sort and control the operation of each screw rod-with the further transfer rate of control mud 20 of inactive time.
Screw rod in the bottom of hopper 620 is disposed in the level of hopper one end, vertical collection screw rod 624.To collect screw rod 24 be used for collecting mud 620, and it is passed to one of two sludge pumps 626 from conveying screw rod.Screw rod 624 can have structure and the motor arrangement that is similar to conveying screw rod.Collect screw rod 624 and preferably have the size that the mud of maximum demand transmission speed is provided.Screw rod 624 is collected in preferred design, with operation in any direction, thereby provides mud to suck moving of position to different pumps.Outlet orifice is installed in bottom at the screw rod shell, mud is guided into the sludge pump 626 of present operation.
From collecting the pump orifice of screw rod 24 shells, vertical pipeline (24 ") are installed preferably to sludge pump 626.Preferably, rotation agglomerate crusher 628 is installed in this pipeline.Agglomerate crusher 628 is rotating paddle and the trellis system that promote that being suitable for semi solid sludge 620 is operated under the mobile speed of pump 626.The agglomerate crusher has two kinds of major functions: 1) will be in mud 620 any megalump fragmentation become littler, more manageable fritter and 2) before any little tramp material can arrive pump 626, they are caught.Agglomerate crusher 628 has additional benefits: give mud 620 shearing forces, with breaking of the polymer binder of beginning in sludge cake.
Preferably before the agglomerate crusher, water 630 is injected in the sludge stream 620.Water 630 helps the liquefaction of mud 620, and is controlled, so that needed final sludge concentration to be provided.Preferably water 630 comprises the recirculated water of technology Venturi scrubber, and its pH is about 2.5 to 4.0.Preferably with water 630 to equal at least 10% needed reactor flow, more preferably the speed of at least 15% and most preferably at least 20% reactor flow adds.In one embodiment, this flow velocity is about 22.9% needed reactor flow.
In another embodiment, preferably, also iron protoxide 632 and sulfuric acid 634 are added in the current 630 in the technology storage tank 636.This adding makes and need be added in the mud and the slurry of generation is not stopped up or the water yield of blocking cruciform joint or tubular reactor minimizes.In one embodiment, technology storage tank 636 is stainless steel-lined concrete pits, and it is of a size of about 11 ' x11 ' x11 '.In technology storage tank 636, sulfuric acid 634 generates ferrous sulfate with iron protoxide 632 reactions, makes that the pH that obtains before mixture is in being added to biosolids is about 2.0 to 2.5.Alternatively, use ferric oxide and and sulfuric acid reaction, generate ferric sulfate, make that the pH that obtains before mixture is in being added to biosolids is about 2.0 to 2.5.Mixture in storage tank stirs with vertical stirrer 638.
The mud of shearing is disposed to the pump orifice that mud transmits pump 42 from agglomerate crusher 628.Sludge pump 40 drains into 8, and " the stainless steel collector, it flows in the high-speed mixing groove 42.Before arriving tempering tank 644, sulfuric acid 646 is injected in the flow, with the pH that controls final mud mixture in 3.0 to 3.5 scope.It is about 1.75% total reactor feeding rate that vitriolic adds speed.
Mud/acid mixture flows into the bottom of shear-mixed groove 642.In one embodiment, shear-mixed groove 642 is vertical and cylindrical grooves of 890 gallons, and it has at a high speed, high-shear gyratory shaker 648, is enough to produce the enough shearings of acidifying biosolids mixture.
In one embodiment, it is that volume is 14,800 gallons a groove that slurry keeps groove, and has the stainless steel structure.It contains the vertical stirrer 650 with two cover blades.Design keeps groove 650, being that slurry feeding provides about 2 hours storage under the feeding rate of maximum.It is operated, and to keep 3.0 to 4.0 pH, wherein solids content is 15% to 28% solid, preferred 20% to 23%.
Extract reactor feed out enter slurry feeding pump 652 pump orifice from maintenance groove 50 bottoms continuously.Control sewage sludge feed speed by the electromotor velocity of regulating slurry feeding pump 652 to reactor.
Figure 6 shows that a kind of method that before mud is as described in Figure 1 made fertilizer with acid and ammonia react, in mud, adds iron sulfate (ferric sulfate).Except the form with ferriferous oxide (ferric oxide) adds in mud the iron, can also in mud, add iron with other form, for example comprise ferric sulfate, metallic iron, iron carbonate and tertiary iron phosphate.Before making fertilizer, change described iron into ferric sulfate with acid and ammonia react.
In one embodiment, the ferriferous oxide (ferric oxide) that in containing water and vitriolic tempering tank, adds powder type.Water and sulfuric acid can comprise the waste water from the exhaust washing system that contains water, sulfuric acid and ammonium sulfate.In this tempering tank, add sulfuric acid ferric oxide is transformed into iron sulfate (ferric sulfate).Then, the ferric sulfate that will be in water and the mixture of ammonium sulfate are added in the biosolids slurry, to promote to improve product hardness and smell.
Except iron, can also add other metal-salt to slurry before the reaction, zinc oxide for example is to reach similar benefit described herein.
Be surprisingly found out that,, can produce the remarkable improvement of mud to the fertilizer process by in mud, adding metal-salt such as ferric sulfate or zinc sulfate or sal epsom.Preferably, in mud, add enough metal-salts,, contain the metal-salt of 0.1 weight % to 10 weight % such as the fertilizer of ferric sulfate with manufacturing as ferrous salt or molysite.More preferably, final fertilizer product contains metal-salt such as the ferric sulfate of 0.5 weight % to 5 weight %.The adding of iron makes more easily to be controlled this method and to provide various other improvement to this method.These improvement comprise:
A) Chemical bond metal such as iron in product.Metal such as iron can with the ammonium sulfate complexing that exists in organic components in the mixture and the mixture.
B) bond such as iron or zinc are with the reduction-sulfurization compound.This bonded is the result be, these reductive sulphur compounds more can not evaporate in atmosphere or the environment, therefore significantly reduced the smell of product sensation.
C) hardness of increase product particle.The pulverizing weight of product increases to significantly from about 4 to 5 pounds and surpasses 6 pounds, more preferably above 7 pounds.Also measure the particle that the present invention is created in 8 to 9 pounds of durometer levels.
D) reduce the dust relevant, feasible storage and the conveying that has improved product with product.
E) smell of reduction product, this will improve the production marketing of product in commodity and special fertilizer commerce.
F) reduce the volatility of nitrogen, make when whole fertilizer product being used on the ground Tanaka of pan soil, reduced the nitrogen amount that is lost in the atmosphere significantly, particularly when being used for commercial fertilizer and putting into practice, compare up to 40% volatility with urea.
G) with before the biosolids slurry mixes, the oxidation ferrous acid is changed into ferric sulfate.
H) utilizability of metal is as iron or zinc, as the micro-nutrient that increases.This is owing to add metal-salt in mixture, but also because combining of the organic constituent of metal and mixture makes metal such as the iron solubleness in water be improved.
I) compare with the product of routine, obtain more oligosaprobic product.Metal-salt such as iron protoxide or ferric oxide, or ferrous sulfate or ferric sulfate carried out pre-treatment before it is added to the biosolids slurry.This pre-treatment is transformed into the black compound with iron, and has avoided red polluting property, and described red polluting property is that the iron phase with the form of iron oxide that adds in advance closes.
Product constructed in accordance is in conjunction with the number of chemical conversion product, and described chemical conversion thing is the important component of final fertilizer.Make before mixture passes through pipe cross reactor, iron adds the multiple condition that causes in mixture in conjunction with vitriolic in " pre-treatment " of mixture, and described condition is as follows to the chemical constitution influence of the operation of pipe cross reactor and finished product:
A) it has improved the reaction kinetics of pipe cross reactor.
B) it causes the enhanced granulation.
C) chemical hydrolysis of the organic molecule in the beginning mud slurry, for example protein is to peptide and amino acid whose conversion, and/or lipid is to the conversion of component molecule such as lipid acid.The chemical hydrolysis of long-chain organic molecule such as protein, carbohydrate, lipid and nucleic acid produced easier can with iron bonded molecule; Its soil microorganisms that can be centered around the root area of target farm crop easilier absorbs, and can more easily directly be absorbed by root of target farm crop and coring institute, makes farm crop be benefited, and has vitality, growth and the productivity of increase.In addition, by the method for hydrolysis relevant with the operation of pipe cross reactor, the hydrolysis of organic molecule makes finished product than there not being under this hydrolysis situation the organic finished product of the biosolids of merging safer.An example of this respect will be the hydrolysis that internal secretion hinders immunomodulator compounds, and described compound has been shown as the endocrine hormone class of imitation at environment, and influences the sex of animal such as crocodile and frog.The destruction of these compounds will increase the public and science confidence, i.e. the use of biosolids product is safe for public health.
D) the reductive sulphur compound is displaced out from the biosolids slurry, make that these odor sources no longer are the components of finished product, or the component that reduces.
E) reduced the viscosity of biosolids slurry, made that the operation of pipe cross reactor is more controlled.
F) improve the mixing that in pipe cross reactor, takes place.
For a person skilled in the art, consider specification sheets of the present invention and practice disclosed herein, other embodiment of the present invention and purposes will be clearly.All reference cited herein, comprise all U.S. and foreign patent and patent application, comprise U.S. Provisional Application 60/473,198 reach the corresponding non-provisional application of meanwhile submitting to, U.S. Patent application 08/852,663,09/735,768 and 09/416,370, be combined in this by reference and specifically and fully.Be intended that think specification sheets and
Embodiment only is exemplary.
Claims (43)
1. make the method for granular nitrogenous fertilizer by organic substance for one kind, this method comprises and adds metal-salt to form slurry in described organic substance.
2. the process of claim 1 wherein that described organic substance comprises biosolids.
3. the process of claim 1 wherein that described slurry comprises the biosolids of dehydration.
4. the method for claim 3, wherein the dehydrating slurry of biosolids contains washer water.
5. the process of claim 1 wherein that described metal-salt comprises molysite, zinc salt or their mixture.
6. the method for claim 5, wherein said molysite comprises ferric sulfate or ferric oxide.
7. the method for claim 5, wherein said zinc salt comprises zinc sulfate or zinc oxide.
8. the process of claim 1 wherein described metal-salt is mixed the generation acidified metal salt with acid.
9. the method for claim 8 wherein adds described acidified metal salt with the amount that is enough to reduce described slurry viscosity.
10. the process of claim 1 wherein under enough concentration and denseness and to mix described slurry forming fluid that described fluid does not hinder flowing of in operating process slurry.
11. the method for claim 1, this method also comprises adding sulfuric acid.
12. the method for claim 11, wherein in being added to described organic substance before, described sulfuric acid is mixed with described metal-salt.
13. the method for claim 11 is wherein mixed described sulfuric acid with iron protoxide, to generate ferrous sulfate, make that the final pH of described slurry is about 2.0 to 2.5.
14. the method for claim 11 is wherein mixed described sulfuric acid with ferric oxide, to generate ferric sulfate, make that the final pH of described slurry is about 2.0 to 2.5.
15. the method for claim 11, wherein said metal-salt comprises acidifying ferric sulfate or ferrous sulfate, it mixes with described organic substance, makes to have enough iron, has fertilizer product by dry weight 0.1 weight % to 10 weight % iron sulfate in generation.
16. the method for claim 15, wherein said fertilizer product have the iron sulfate by dry weight 0.5 weight % to 5 weight %.
17. the method for claim 15, wherein said fertilizer product have the iron sulfate by dry weight 1 weight % to 3 weight %.
18. the method for claim 11 wherein is added to described sulfuric acid in the described organic substance before it arrives tempering tank and with the speed of about 1.75% total feed rate, to obtain 3.0 to 3.5 pH scope.
19. the process of claim 1 wherein slurry is pumped in the shear-mixed groove that contains the high-shear gyratory shaker that described stirrer is to be enough to produce the speed rotation of high shear force.
20. the method for claim 19, this method also comprise described slurry is passed to maintenance or the compensating groove that contains stirrer from described shear-mixed groove.
21. the method for claim 20, wherein said maintenance or the compensating groove that contains stirrer can provide about 2 hours storage for slurry.
22. the method for claim 20 is wherein operated described maintenance or compensating groove, being that to keep pH under 15% to the 28% solid situation be 3.0 to 4.0 in solids content.
23. the method for claim 22, wherein said solids content are 20% to 23%.
24. the process of claim 1 wherein that described metal-salt combines with one or more element chemistries of slurry.
25. the method for claim 24, wherein said metal-salt is a molysite, and it combines with the ammonium sulfate or the ammonium phosphate that exist in the described slurry.
26. the process of claim 1 wherein that described metal-salt comprises acidifying ferrous salt or molysite, with the sulphur compound of reduction in described slurry.
27. the method for claim 26, wherein said acidifying ferrous salt or molysite reduce the formation of dust in the operating process.
28. the method for claim 26, wherein said acidifying ferrous salt or molysite reduce the smell in the operating process.
29. the process of claim 1 wherein and add the granulation formation that described metal-salt has improved described slurry.
30. the process of claim 1 wherein that described metal-salt has caused the chemical hydrolysis of the organic molecule in the described slurry.
31. the process of claim 1 wherein that described metal-salt displaces organic substance with the reductive sulphur compound, thereby reduce the repugnant substance source in fertilizer product.
32. the process of claim 1 wherein described metal-salt is added in the described organic substance in pipe cross reactor.
33. the method for claim 32, wherein said metal-salt has improved the kinetics of described pipe cross reactor.
34. the method for claim 32, wherein said metal-salt has reduced the viscosity of described slurry, makes that the operation of described pipe cross reactor is more controlled than the situation that does not have metal-salt.
35. the process of claim 1 wherein described metal-salt is added in the tubular reactor.
36. fertilizer product of making by the method for claim 1.
37. the product of claim 36, wherein said metal-salt are acidifying ferrous salt or molysite.
38. the product of claim 37, wherein said acidifying ferrous salt or molysite improve product hardness.
39. the product of claim 36, it pulverizes weight greater than 6 pounds.
40. the product of claim 39, it pulverizes weight greater than 7 pounds.
41. the product of claim 36, the metal of wherein said metal-salt are utilizable for plant.
42. the product of claim 41, the solubleness of wherein said metal in water is improved.
43. the product of claim 36, it is low polluted product.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
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| US47319703P | 2003-05-27 | 2003-05-27 | |
| US60/473,197 | 2003-05-27 | ||
| US60/473,198 | 2003-05-27 |
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| CN1856455A true CN1856455A (en) | 2006-11-01 |
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| CN104245631A (en) * | 2011-03-28 | 2014-12-24 | 维塔格控股有限责任公司 | High value organic-enhanced inorganic fertilizers |
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| CN104245631A (en) * | 2011-03-28 | 2014-12-24 | 维塔格控股有限责任公司 | High value organic-enhanced inorganic fertilizers |
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