MD4382C1 - Combined biogas-production reactor - Google Patents
Combined biogas-production reactor Download PDFInfo
- Publication number
- MD4382C1 MD4382C1 MDA20140087A MD20140087A MD4382C1 MD 4382 C1 MD4382 C1 MD 4382C1 MD A20140087 A MDA20140087 A MD A20140087A MD 20140087 A MD20140087 A MD 20140087A MD 4382 C1 MD4382 C1 MD 4382C1
- Authority
- MD
- Moldova
- Prior art keywords
- biogas
- communicates
- valves
- electromagnetic valve
- reactor
- Prior art date
Links
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 239000002028 Biomass Substances 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000001471 micro-filtration Methods 0.000 claims abstract description 13
- 238000011068 loading method Methods 0.000 claims abstract description 5
- 238000012544 monitoring process Methods 0.000 claims abstract description 4
- 238000009434 installation Methods 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 6
- 239000010802 sludge Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 abstract description 9
- 238000012545 processing Methods 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 2
- 210000002445 nipple Anatomy 0.000 abstract 4
- 239000000084 colloidal system Substances 0.000 abstract 1
- 239000010865 sewage Substances 0.000 abstract 1
- 239000002002 slurry Substances 0.000 abstract 1
- 238000000855 fermentation Methods 0.000 description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 230000004151 fermentation Effects 0.000 description 9
- 239000012528 membrane Substances 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 238000005755 formation reaction Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000003851 biochemical process Effects 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- 244000005706 microflora Species 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 230000000696 methanogenic effect Effects 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- YYGNTYWPHWGJRM-UHFFFAOYSA-N (6E,10E,14E,18E)-2,6,10,15,19,23-hexamethyltetracosa-2,6,10,14,18,22-hexaene Chemical compound CC(C)=CCCC(C)=CCCC(C)=CCCC=C(C)CCC=C(C)CCC=C(C)C YYGNTYWPHWGJRM-UHFFFAOYSA-N 0.000 description 1
- 241000283690 Bos taurus Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- BHEOSNUKNHRBNM-UHFFFAOYSA-N Tetramethylsqualene Natural products CC(=C)C(C)CCC(=C)C(C)CCC(C)=CCCC=C(C)CCC(C)C(=C)CCC(C)C(C)=C BHEOSNUKNHRBNM-UHFFFAOYSA-N 0.000 description 1
- ZNUAKACHFYTNFX-UHFFFAOYSA-N Wallichenol Natural products CC12CCC(O)C(C)(C)C1CCC1(C)C2CCC2C3C(C(=C)CO)CCC3(C)CCC21C ZNUAKACHFYTNFX-UHFFFAOYSA-N 0.000 description 1
- 230000000789 acetogenic effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- FVWJYYTZTCVBKE-ROUWMTJPSA-N betulin Chemical compound C1C[C@H](O)C(C)(C)[C@@H]2CC[C@@]3(C)[C@]4(C)CC[C@@]5(CO)CC[C@@H](C(=C)C)[C@@H]5[C@H]4CC[C@@H]3[C@]21C FVWJYYTZTCVBKE-ROUWMTJPSA-N 0.000 description 1
- MVIRREHRVZLANQ-UHFFFAOYSA-N betulin Natural products CC(=O)OC1CCC2(C)C(CCC3(C)C2CC=C4C5C(CCC5(CO)CCC34C)C(=C)C)C1(C)C MVIRREHRVZLANQ-UHFFFAOYSA-N 0.000 description 1
- 230000000975 bioactive effect Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000004071 biological effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- PRAKJMSDJKAYCZ-UHFFFAOYSA-N dodecahydrosqualene Natural products CC(C)CCCC(C)CCCC(C)CCCCC(C)CCCC(C)CCCC(C)C PRAKJMSDJKAYCZ-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000004941 influx Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 238000009629 microbiological culture Methods 0.000 description 1
- 230000001717 pathogenic effect Effects 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229940031439 squalene Drugs 0.000 description 1
- TUHBEKDERLKLEC-UHFFFAOYSA-N squalene Natural products CC(=CCCC(=CCCC(=CCCC=C(/C)CCC=C(/C)CC=C(C)C)C)C)C TUHBEKDERLKLEC-UHFFFAOYSA-N 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 230000004936 stimulating effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
- 150000003648 triterpenes Chemical class 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Treatment Of Sludge (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
Description
Invenţia se referă la instalaţii pentru obţinerea biometanului în componenţa biogazului şi poate fi utilizată în diferite ramuri ale agriculturii şi în industria de prelucrare pentru epurarea apelor reziduale şi obţinerea biogazului. The invention refers to installations for obtaining biomethane in the composition of biogas and can be used in various branches of agriculture and in the processing industry for the purification of waste water and obtaining biogas.
Este cunoscut bioreactorul pentru obţinerea biogazului, care include un modul de membrane pentru microfiltrare, care permite separarea fracţiei micromoleculare şi dispersarea fină a apei uzate tratate [1]. The bioreactor for obtaining biogas is known, which includes a membrane module for microfiltration, which allows the separation of the micromolecular fraction and the fine dispersion of the treated wastewater [1].
Dezavantajul acestui bioreactor constă în aceea că la exploatarea lui apar unele dificultăţi din cauza colmatării microporilor membranelor cu particule solide şi microorganisme. The disadvantage of this bioreactor lies in the fact that some difficulties arise during its operation due to the clogging of the micropores of the membranes with solid particles and microorganisms.
Cea mai apropiată soluţie este reactorul combinat de obţinere a biogazului, care include un corp cilindric cu fund conic cu o încărcătură în interior, dotat cu conducte de alimentare şi evacuare a lichidului, sistem de evacuare a biogazului, capac cu manometru cu contacte electrice, bloc de comandă, sistem de recirculare a biomasei şi ventile electromagnetice [2]. The closest solution is the combined biogas reactor, which includes a cylindrical body with a conical bottom with a charge inside, equipped with liquid supply and discharge pipes, biogas discharge system, manometer cover with electrical contacts, block control system, biomass recirculation system and electromagnetic valves [2].
Dezavantajele acestui reactor constau în eficienţa redusă a tratării biochimice şi caracterul complex al procesului de fermentare anaerobă a biomasei. The disadvantages of this reactor consist in the low efficiency of the biochemical treatment and the complex character of the process of anaerobic fermentation of biomass.
Problema tehnică pe care o rezolvă prezenta invenţie constă în majorarea gradului de utilizare a biomasei, eficienţei procesului de fermentare, precum şi a gradului de epurare a lichidului tratat şi deversat pentru a fi utilizat. The technical problem that the present invention solves consists in increasing the degree of use of biomass, the efficiency of the fermentation process, as well as the degree of purification of the liquid treated and discharged to be used.
Reactorul combinat pentru obţinerea biogazului înlătură dezavantajele menţionate mai sus prin aceea că include un corp cilindric cu fund conic, unit cu un ştuţ cu un ventil pentru evacuarea nămolului, o conductă de alimentare cu un ventil electromagnetic, care comunică cu o moară coloidală cu un dispozitiv de încărcare a biomasei, şi un ştuţ de evacuare a lichidului, un capac, partea superioară a căruia este dotată cu un sistem de evacuare a biogazului, care conţine un închizător hidraulic cu clopot, un ventil electromagnetic şi un senzor de monitorizare a conţinutului de CO2 în biogaz, instalat pe un ştuţ de evacuare a biogazului, totodată pe partea superioară a capacului este instalat un manometru cu contacte electrice. În interiorul corpului sunt amplasate o încărcătură şi un indicator de nivel cu contacte electrice. Reactorul mai include un sistem de recirculare, care conţine o pompă, unită cu ştuţul de evacuare a lichidului, şi comunică cu nişte conducte de repartizare cu nişte ventile electromagnetice, totodată conductele de repartizare prin intermediul ventilelor electromagnetice sunt unite cu o instalaţie de microfiltrare, care conţine un ejector, care prin intermediul unei conducte auxiliare de gaz cu un ventil electromagnetic comunică cu corpul, o conductă de ocolire cu nişte ventile, care prin intermediul unui traductor de viteză a fluxului de lichid comunică cu o conductă de recirculare, amplasată în partea inferioară a corpului, şi o conductă de evacuare cu un ventil electromagnetic. De asemenea reactorul conţine un bloc de comandă pentru dirijarea automată a procesului de obţinere a biogazului, la care sunt unite ventilele, senzorul, manometrul, moara, indicatorul de nivel şi traductorul. The combined reactor for obtaining biogas removes the disadvantages mentioned above in that it includes a cylindrical body with a conical bottom, joined with a nozzle with a valve for the discharge of sludge, a feed pipe with an electromagnetic valve, which communicates with a colloidal mill with a device of biomass loading, and a liquid outlet spigot, a cover, the upper part of which is equipped with a biogas outlet system, which contains a hydraulic valve with a bell, an electromagnetic valve and a sensor for monitoring the CO2 content in biogas, installed on a biogas outlet nozzle, at the same time a manometer with electrical contacts is installed on the upper part of the cover. A load and a level indicator with electrical contacts are placed inside the body. The reactor also includes a recirculation system, which contains a pump, connected to the liquid outlet nozzle, and communicates with distribution pipes with electromagnetic valves, at the same time, the distribution pipes through the electromagnetic valves are connected to a microfiltration installation, which contains an ejector, which through an auxiliary gas pipe with an electromagnetic valve communicates with the body, a bypass pipe with some valves, which through a liquid flow velocity transducer communicates with a recirculation pipe, located in the lower part of the body, and an exhaust pipe with an electromagnetic valve. The reactor also contains a control block for the automatic management of the biogas production process, to which the valves, the sensor, the manometer, the mill, the level indicator and the transducer are connected.
Rezultatul tehnic constă în posibilitatea intensificării procesului biochimic în condiţiile unei presiuni ridicate în reactor, care determină creşterea concentraţiei componentelor, care interacţionează datorită reducerii volumului fazei gazoase în conformitate cu legea lui Le Chatelier. Datorită prezenţei morii coloidale se asigură posibilitatea dispersării fine a suspensiilor mecanice din biomasă până la dimensiuni ale celor mai mari particule ce nu depăşesc 1…0,005 µm cu distrucţia structurilor macromoleculare şi accesibilitatea microorganismelor pentru transformările biochimice în biomasă. Aceasta, la rândul său, majorează eficienţa fermentării anaerobe a biomasei şi asigură posibilitatea separării prin microfiltrare a fazelor solidă şi coloidală. The technical result consists in the possibility of intensifying the biochemical process under conditions of high pressure in the reactor, which determines the increase in the concentration of the components, which interact due to the reduction of the volume of the gaseous phase in accordance with Le Chatelier's law. Due to the presence of the colloidal mill, the possibility of fine dispersion of mechanical biomass suspensions is ensured up to the size of the largest particles that do not exceed 1...0.005 µm with the destruction of macromolecular structures and the accessibility of microorganisms for biochemical transformations in biomass. This, in turn, increases the efficiency of the anaerobic fermentation of the biomass and ensures the possibility of separating the solid and colloidal phases by microfiltration.
Invenţia se explică prin desenul din figură, care reprezintă schema reactorului combinat pentru obţinerea biogazului. The invention is explained by the drawing in the figure, which represents the scheme of the combined reactor for obtaining biogas.
Reactorul combinat pentru obţinerea biogazului include un corp cilindric cu fund conic 1, unit cu un ştuţ 11 cu un ventil 12 pentru evacuarea nămolului, o conductă de alimentare 4 cu un ventil electromagnetic 25, care comunică cu o moară coloidală 6 cu un dispozitiv de încărcare a biomasei 5, şi un ştuţ 13 de evacuare a lichidului, un capac 7, partea superioară a căruia este dotată cu un sistem de evacuare a biogazului, care conţine un închizător hidraulic cu clopot 9, un ventil electromagnetic 26 şi un senzor 10 de monitorizare a conţinutului de CO2 în biogaz, instalat pe un ştuţ 32 de evacuare a biogazului, totodată pe partea superioară a capacului 7 este instalat un manometru 8 cu contacte electrice. În interiorul corpului 1 sunt amplasate o încărcătură 2 şi un indicator de nivel 3 cu contacte electrice. Reactorul mai include un sistem de recirculare, care conţine o pompă 14, unită cu ştuţul 13 de evacuare a lichidului, şi comunică cu nişte conducte de repartizare 15 cu nişte ventile electromagnetice 27, 28, totodată conductele de repartizare 15 prin intermediul ventilelor electromagnetice 27, 28 sunt unite cu o instalaţie de microfiltrare 16, care conţine un ejector 19, care prin intermediul unei conducte auxiliare de gaz 20 cu un ventil electromagnetic 29 comunică cu corpul 1, o conductă de ocolire 17 cu nişte ventile 18, 31, care prin intermediul unui traductor 22 de viteză a fluxului de lichid comunică cu o conductă de recirculare 21, amplasată în partea inferioară a corpului 1, şi o conductă de evacuare 23 cu un ventil electromagnetic 30. De asemenea reactorul conţine un bloc de comandă 24 pentru dirijarea automată a procesului de obţinere a biogazului, la care sunt unite ventilele 25, 26, 27, 28, 29, 30, 31, senzorul 10, manometrul 8, moara 6, indicatorul de nivel 3 şi traductorul 22. The combined reactor for obtaining biogas includes a cylindrical body with a conical bottom 1, connected with a nozzle 11 with a valve 12 for the discharge of sludge, a supply pipe 4 with an electromagnetic valve 25, which communicates with a colloidal mill 6 with a loading device of biomass 5, and a nozzle 13 for liquid evacuation, a cover 7, the upper part of which is equipped with a biogas evacuation system, which contains a hydraulic shutter with a bell 9, an electromagnetic valve 26 and a monitoring sensor 10 of the CO2 content in the biogas, installed on a biogas discharge nozzle 32, at the same time a manometer 8 with electrical contacts is installed on the upper part of the cover 7. A load 2 and a level indicator 3 with electrical contacts are placed inside the body 1. The reactor also includes a recirculation system, which contains a pump 14, connected to the liquid discharge nozzle 13, and communicates with some distribution pipes 15 with some electromagnetic valves 27, 28, also the distribution pipes 15 by means of electromagnetic valves 27, 28 are connected to a microfiltration installation 16, which contains an ejector 19, which through an auxiliary gas pipe 20 with an electromagnetic valve 29 communicates with body 1, a bypass pipe 17 with some valves 18, 31, which through a liquid flow velocity transducer 22 communicates with a recirculation pipe 21, located in the lower part of the body 1, and an exhaust pipe 23 with an electromagnetic valve 30. The reactor also contains a control block 24 for the automatic routing of of the biogas production process, to which valves 25, 26, 27, 28, 29, 30, 31, sensor 10, manometer 8, mill 6, level indicator 3 and transducer 22 are connected.
Reactorul combinat pentru obţinerea biogazului funcţionează în modul următor. The combined reactor for obtaining biogas works in the following way.
În dispozitivul de încărcare 5 se introduce biomasă, de exemplu, amestec de borhot de alcool cu microadaos stimulent de substanţe bioactive (sau microadaos de fitocatalizatori naturali, pentru fermentarea anaerobă, şi bălegar de vite mari cornute), se pune în funcţiune moara coloidală 6 în care se produce secţionarea biomasei şi mărunţirea fină ulterioară până la dispersia mai mică de 1 µm cu formarea unor structuri coloidale stabile şi apoi, la deschiderea ventilului 25, sub presiune are loc curgerea biomasei dispersate în conducta 4 şi umplerea corpului 1 al reactorului până la nivelul stabilit de indicatorul de nivel 3, care cu ajutorul blocului de comandă 24 întrerupe provizoriu introducerea biomasei, după care reactorul se încălzeşte până la o temperatură optimă de 33±2°C. Biomass is introduced into the loading device 5, for example, a mixture of alcohol borhot with a stimulating microaddition of bioactive substances (or a microaddition of natural phytocatalysts, for anaerobic fermentation, and dung of large horned cattle), the colloidal mill 6 is put into operation in which produces the sectioning of the biomass and the subsequent fine shredding until the dispersion is less than 1 µm with the formation of stable colloidal structures and then, when the valve 25 is opened, under pressure the flow of the dispersed biomass takes place in the pipe 4 and the filling of the body 1 of the reactor up to the level set by level indicator 3, which with the help of control block 24 temporarily interrupts the introduction of biomass, after which the reactor heats up to an optimal temperature of 33±2°C.
Datorită emisiei de biogaz la închiderea ventilelor 25, 26, 27 şi 28, are loc creşterea presiunii în reactor până la valoarea stabilită. Gazele emise ridică presiunea în reactor, care este înregistrată de manometrul 8 cu contacte electrice, iar pe măsura atingerii valorii stabilite se include în lucru blocul de comandă 24, care deschide ventilele 25 şi 26, asigurând introducerea porţiilor de biomasă şi, în consecinţă, regimul continuu de funcţionare a reactorului. Prezenţa încărcăturii 2 în reactor asigură fixarea microflorei pe suprafaţa ei, ceea ce preîntâmpină pierderea ei şi intensifică procesul de producere a biogazului. Imobilizarea celulelor microorganismelor pe suprafaţa încărcăturii 2 conduce la o concentraţie mare a microflorei active şi, respectiv, la participarea multiplă a celulelor microbiene, favorizează adaptarea lor la afluxul variabil al poluanţilor şi majorarea capacităţii lor catalitice, totodată exclude necesitatea separării microflorei de lichidul tratat în scopul recirculării ei în reactor. Apoi se include pompa 14, se deschid ventilele 27 şi 28 şi începe să funcţioneze instalaţia de microfiltrare 16, efectuând separarea fazei lichide, care se evacuează prin conducta 23 spre utilizare, şi separarea părţii macromoleculare şi mecanice a biomasei, care sub presiune se întoarce în corpul 1 pentru continuarea procesului de fermentare microbiologică. Această separare a fazelor prin microfiltrare asigură nu numai o curăţire mai eficientă a lichidului, dar şi o creştere a randamentului utilizării biomasei în procesul de producere a biogazului. Due to the emission of biogas when valves 25, 26, 27 and 28 are closed, the pressure in the reactor increases to the set value. The emitted gases raise the pressure in the reactor, which is registered by the manometer 8 with electrical contacts, and as soon as the set value is reached, the control block 24 is included in the work, which opens the valves 25 and 26, ensuring the introduction of the biomass portions and, consequently, the regime continuous operation of the reactor. The presence of charge 2 in the reactor ensures the fixation of the microflora on its surface, which prevents its loss and intensifies the biogas production process. The immobilization of microorganism cells on the surface of load 2 leads to a high concentration of active microflora and, respectively, to the multiple participation of microbial cells, favors their adaptation to the variable influx of pollutants and increases their catalytic capacity, at the same time excludes the need to separate the microflora from the treated liquid for the purpose its recirculation in the reactor. Then the pump 14 is turned on, the valves 27 and 28 are opened and the microfiltration installation 16 starts working, separating the liquid phase, which is evacuated through the pipe 23 for use, and the separation of the macromolecular and mechanical part of the biomass, which under pressure returns to body 1 to continue the microbiological fermentation process. This separation of phases by microfiltration ensures not only a more efficient cleaning of the liquid, but also an increase in the yield of biomass use in the biogas production process.
Astfel, dacă în condiţiile când se reuşeşte utilizarea a 60% de biomasă pentru producerea biogazului la fermentarea anaerobă, 40% rămân neutilizate, atunci prin sistemul de microfiltrare şi recirculare a biomasei nefermentate în procesul metanogen randamentul utilizării ei se ridică până la 85…95%. Thus, if in the conditions when 60% of biomass is used for the production of biogas during anaerobic fermentation, 40% remains unused, then through the system of microfiltration and recirculation of unfermented biomass in the methanogenic process, the yield of its use rises to 85...95% .
Separarea fazelor prin membrane în instalaţia de microfiltrare asigură înlăturarea practic totală a culturilor microbiene în interiorul reactorului, inclusiv a agenţilor patogeni, ceea ce permite majorarea concentraţiei microflorei în reactoare şi degradarea maximă a anumitor genuri de poluanţi greu biodegradabili concomitent cu dezinfecţia apelor uzate tratate. The separation of phases through membranes in the microfiltration installation ensures the practically total removal of microbial cultures inside the reactor, including pathogenic agents, which allows increasing the concentration of microflora in the reactors and the maximum degradation of certain types of hard-to-biodegrade pollutants simultaneously with the disinfection of the treated wastewater.
O acţiune importantă a sistemului de recirculare a biomasei este fluidizarea, ceea ce intensifică procesele de schimb şi transfer de masă în volumul reactorului, precum şi uniformizarea temperaturii, creând condiţii optime mezofile de fermentare în el. An important action of the biomass recirculation system is fluidization, which intensifies the mass exchange and transfer processes in the reactor volume, as well as temperature uniformity, creating optimal mesophilic fermentation conditions in it.
Desfăşurarea procesului de fermentare anaerobă sub presiune ridicată în reactor, în comparaţie cu cel care are loc la presiune obişnuită, prezintă un factor important în procesul biochimic, care influenţează atât viteza reacţiilor omogene gazoase ce condiţionează formarea biometanului, cât şi producţia lui, ridicând conţinutul acestuia în componenţa biogazului. The performance of the anaerobic fermentation process under high pressure in the reactor, compared to the one that takes place at normal pressure, presents an important factor in the biochemical process, which influences both the speed of the homogeneous gaseous reactions that condition the formation of biomethane, as well as its production, raising its content in the biogas composition.
Astfel, o particularitate a desfăşurării procesului de fermentare în prima fază acetogenă este legată de emisia primară a hidrogenului molecular, apoi a CO şi CO2, care în faza metanogenă, în afară de un şir de alte procese biochimice, se transformă în metan conform reacţiilor de ordin general: Thus, a peculiarity of the fermentation process in the first acetogenic phase is related to the primary emission of molecular hydrogen, then of CO and CO2, which in the methanogenic phase, apart from a series of other biochemical processes, transforms into methane according to the reactions of general order:
CO + 3H2 → CH4+H2O şi CO2 + 4H2 → СН4+2Н2О CO + 3H2 → CH4+H2O and CO2 + 4H2 → СН4+2Н2О
De aceea condiţiile de presiune ridicată în reactor sunt un factor intensificator, datorită majorării concentraţiei componentelor, care interacţionează din contul reducerii volumului fazei gazoase. Totodată, conform stoechiometriei reacţiilor menţionate de formare a metanului, în conformitate cu legea lui Le Chatelier la interacţiunea CO şi CO2 pentru formarea unui mol de CH4, sunt necesari 3 şi 4 moli de H2, corespunzător. De aceea concentraţiile echilibrate ale componentelor iniţiale se micşorează, iar procesul are loc cu reducerea volumului. În legătură cu aceasta, majorarea presiunii în reactor ridică concentraţia şi viteza reacţiei gazoase, iar producţia de biometan în aceste condiţii este în continuă creştere. Experimental este stabilit că din contul majorării presiunii în reactor, conform invenţiei, cantitatea de metan în componenţa biogazului creşte de la 60…65% până la 90…95% şi mai mult, restul îl reprezintă CO2. Ca rezultat, observăm că particularităţile constructive ale invenţiei permit intensificarea procesului biochimic de fermentare, ceea ce conduce la creşterea esenţială a conţinutului de biometan în componenţa biogazului în calitate de produs final. That is why the conditions of high pressure in the reactor are an intensifying factor, due to the increase in the concentration of the components, which interact due to the reduction of the volume of the gas phase. At the same time, according to the stoichiometry of the mentioned methane formation reactions, according to Le Chatelier's law for the interaction of CO and CO2 for the formation of one mole of CH4, 3 and 4 moles of H2 are needed, respectively. That is why the balanced concentrations of the initial components decrease, and the process takes place with a reduction in volume. In connection with this, increasing the pressure in the reactor raises the concentration and speed of the gaseous reaction, and the production of biomethane under these conditions is continuously increasing. It is experimentally established that due to the increase in pressure in the reactor, according to the invention, the amount of methane in the biogas composition increases from 60...65% to 90...95% and more, the rest is CO2. As a result, we note that the constructive particularities of the invention allow the intensification of the biochemical process of fermentation, which leads to the essential increase of the biomethane content in the composition of the biogas as a final product.
Un alt factor intensificator, care ridică eficienţa procesului de fermentare anaerobă, este introducerea suplimentară şi distribuţia uniformă în biomasă a microadaosurilor fitostimulente din rândul triterpenelor, în particular a betulinolului, scualenului etc., care posedă o activitate biologică ce influenţează dezvoltarea microorganismelor, majorează energia şi viteza de creştere a consorţiului de bacterii metanogene, intensifică procesul de formare a metanului, ridicând viteza şi durata efectuării reacţiilor biochimice, ceea ce duce la îmbunătăţirea parametrilor tehnologici, care asigură majorarea producţiei de biogaz şi a conţinutului în el de biometan, totodată reducerea duratei de fermentare anaerobă, respectiv, reducând cheltuielile capitale şi de exploatare a reactoarelor. Another intensifying factor, which increases the efficiency of the anaerobic fermentation process, is the additional introduction and uniform distribution in the biomass of phytostimulant microadditions from among triterpenes, in particular betulinol, squalene, etc., which possess a biological activity that influences the development of microorganisms, increases energy and the growth rate of the consortium of methanogenic bacteria intensifies the process of methane formation, increasing the speed and duration of biochemical reactions, which leads to the improvement of technological parameters, which ensure the increase of biogas production and the content of biomethane in it, at the same time reducing the duration of anaerobic fermentation, respectively, reducing the capital and operating expenses of the reactors.
În componenţa instalaţiei de microfiltrare baromembranice pot fi utilizate atât membrane standard din ceramică, cât şi pe bază organică, produse de industrie, cu dimensiunile microporilor de 0,01…0,5 µm, şi cu utilizarea utilajului industrial, de exemplu, a instalaţiei de tip УФ-УМК-30 elaborate de întreprinderea "Alimentarmaş" SRL sau altele. În acelaşi timp, utilizarea elementelor baromembranice necesită regenerarea lor periodică, deoarece cu timpul are loc înfundarea microporilor, ceea ce reduce viteza de penetrare a lichidului, înregistrată de traductorul 22 de viteză a fluxului. Regenerarea membranelor şi restabilirea capacităţii de funcţionare a instalaţiei de microfiltrare se produce conform indicaţiilor traductorului 22 de viteză a fluxului prin comutarea automată de scurtă durată a funcţionării ei şi prin spălarea inversă a micromembranelor. În această perioadă la comanda blocului de comandă 24 se închid ventilele 27, 30 şi 31 şi se deschid ventilele 28 şi 29, în poziţia deschisă a ventilului 18 se include în lucru ejectorul 19, iar amestecul gaz-lichid, plin cu biogazul din spaţiul de gaz al reactorului, se îndreaptă în direcţia opusă a instalaţiei de microfiltrare 16 şi apoi sub presiune excendentă din nou se evacuează prin conducta 21 în reactor. Bulele de gaz creează efectul de barbotare, favorizând fluidizarea suplimentară a biomasei, ceea ce influenţează pozitiv fermentarea biochimică a ei. Utilizarea amestecului prin barbotare în reactor permite reducerea la minim a neuniformităţii temperaturii în reactor şi eliminarea produselor inhibitoare ale activităţii bacteriene, ceea ce este necesar şi important pentru creşterea bacteriilor. In the composition of the baromembrane microfiltration installation, both standard ceramic and organic-based membranes, manufactured by industry, with micropore sizes of 0.01...0.5 µm can be used, and with the use of industrial equipment, for example, the type УФ-УМК-30 developed by the enterprise "Alimentarmaş" SRL or others. At the same time, the use of baromembrane elements requires their periodic regeneration, because over time the micropores become clogged, which reduces the speed of liquid penetration, recorded by the flow rate transducer 22. The regeneration of the membranes and the restoration of the functioning capacity of the microfiltration installation is produced according to the indications of the flow rate transducer 22 by the short-term automatic switching of its operation and by the reverse washing of the micromembranes. During this period, at the command of the control block 24, the valves 27, 30 and 31 are closed and the valves 28 and 29 are opened, in the open position of the valve 18, the ejector 19 is included in the work, and the gas-liquid mixture, filled with the biogas from the space gas of the reactor, it goes in the opposite direction of the microfiltration installation 16 and then under excessive pressure it is again evacuated through the pipe 21 in the reactor. The gas bubbles create the bubbling effect, favoring the additional fluidization of the biomass, which positively influences its biochemical fermentation. The use of the mixture by bubbling in the reactor allows to minimize the non-uniformity of the temperature in the reactor and to eliminate the inhibitory products of the bacterial activity, which is necessary and important for the growth of the bacteria.
Fluxul invers al lichidului prin instalaţia 16 conduce la deschiderea rapidă a microporilor, după ce din nou se închid ventilele 28, 29 şi 18 şi se deschid ventilele 27, 30 şi 31, iar ciclul de filtrare se reia. The reverse flow of the liquid through the installation 16 leads to the rapid opening of the micropores, after the valves 28, 29 and 18 are closed again and the valves 27, 30 and 31 are opened, and the filtration cycle resumes.
Astfel, datorită soluţiei tehnice propuse se obţine majorarea gradului de utilizare a biomasei, eficienţei procesului de fermentare şi gradului de epurare a lichidului tratat la evacuarea lui. Thus, thanks to the proposed technical solution, the increase in the degree of biomass utilization, the efficiency of the fermentation process and the degree of purification of the treated liquid at its discharge is obtained.
1. Visvanathan Ch., AbeynayakaA. Developments and future potentials of anaerobic membrane bioreactors. Membrane water treatment, vol. 3, No 1, 2012 1. Visvanathan Ch., AbeynayakaA. Developments and future potentials of anaerobic membrane bioreactors. Membrane water treatment, vol. 3, No. 1, 2012
2. MD 4376 B1 2015.10.31 2. MD 4376 B1 2015.10.31
Claims (1)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| MDA20140087A MD4382C1 (en) | 2014-08-22 | 2014-08-22 | Combined biogas-production reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| MDA20140087A MD4382C1 (en) | 2014-08-22 | 2014-08-22 | Combined biogas-production reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| MD4382B1 MD4382B1 (en) | 2015-11-30 |
| MD4382C1 true MD4382C1 (en) | 2016-06-30 |
Family
ID=54753225
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| MDA20140087A MD4382C1 (en) | 2014-08-22 | 2014-08-22 | Combined biogas-production reactor |
Country Status (1)
| Country | Link |
|---|---|
| MD (1) | MD4382C1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106836114A (en) * | 2017-01-09 | 2017-06-13 | 中国科学院生态环境研究中心 | Administering method for eliminating rural area type black and odorous water |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4530762A (en) * | 1984-03-28 | 1985-07-23 | Love Leonard S | Anaerobic reactor |
| SU1715715A1 (en) * | 1989-10-25 | 1992-02-28 | Балабановское Отделение Государственного Института По Проектированию Предприятий Деревообрабатывающей Промышленности "Гипролеспром" | Reactor for anaerobic treatment of organic matter and producing methane |
| MD2794G2 (en) * | 2004-09-08 | 2006-01-31 | Государственный Университет Молд0 | Anaerobic bioreactor |
| EP2020434A1 (en) * | 2007-08-03 | 2009-02-04 | ACEA Pinerolese Industriale S.p.A. | Reactor for the anaerobic production of biogas |
| MD4204B1 (en) * | 2012-03-29 | 2013-02-28 | Univ De Stat Din Moldova | Installation for anaerobic production of biohydrogen |
| MD4244C1 (en) * | 2012-06-11 | 2014-02-28 | Государственный Университет Молд0 | Combined anaerobic reactor for the production of biomethane |
| MD4376B1 (en) * | 2014-08-22 | 2015-10-31 | Universitatea De Stat Din Moldova | Combined high-pressure biogas production reactor |
-
2014
- 2014-08-22 MD MDA20140087A patent/MD4382C1/en not_active IP Right Cessation
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4530762A (en) * | 1984-03-28 | 1985-07-23 | Love Leonard S | Anaerobic reactor |
| SU1715715A1 (en) * | 1989-10-25 | 1992-02-28 | Балабановское Отделение Государственного Института По Проектированию Предприятий Деревообрабатывающей Промышленности "Гипролеспром" | Reactor for anaerobic treatment of organic matter and producing methane |
| MD2794G2 (en) * | 2004-09-08 | 2006-01-31 | Государственный Университет Молд0 | Anaerobic bioreactor |
| EP2020434A1 (en) * | 2007-08-03 | 2009-02-04 | ACEA Pinerolese Industriale S.p.A. | Reactor for the anaerobic production of biogas |
| MD4204B1 (en) * | 2012-03-29 | 2013-02-28 | Univ De Stat Din Moldova | Installation for anaerobic production of biohydrogen |
| MD4244C1 (en) * | 2012-06-11 | 2014-02-28 | Государственный Университет Молд0 | Combined anaerobic reactor for the production of biomethane |
| MD4376B1 (en) * | 2014-08-22 | 2015-10-31 | Universitatea De Stat Din Moldova | Combined high-pressure biogas production reactor |
Non-Patent Citations (1)
| Title |
|---|
| Visvanathan Ch., AbeynayakaA. Developments and future potentials of anaerobic membrane bioreactors. Membrane water treatment, vol. 3, No 1, 2012 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106836114A (en) * | 2017-01-09 | 2017-06-13 | 中国科学院生态环境研究中心 | Administering method for eliminating rural area type black and odorous water |
Also Published As
| Publication number | Publication date |
|---|---|
| MD4382B1 (en) | 2015-11-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105621789B (en) | A kind of biogas slurry treatment device and method based on microdisk electrode | |
| CN102965278B (en) | A high-efficiency two-phase anaerobic fermentation device | |
| CN102939369A (en) | Anaerobic reactor | |
| JPS61501195A (en) | Method and apparatus for anaerobically treating organic substrates | |
| CN103880263A (en) | Dynamic membrane forming control method applicable to anaerobic digestion of excess sludge | |
| CN102311281A (en) | Water-gas linkage totally-enclosed rotary type anaerobic fermentation apparatus for municipal solid waste | |
| CN103880252A (en) | Integrated treatment equipment of rural domestic waste | |
| MD4244C1 (en) | Combined anaerobic reactor for the production of biomethane | |
| MD4204C1 (en) | Installation for anaerobic production of biohydrogen | |
| CN201512461U (en) | Anaerobic and aerobic integrated water treatment bioreactor | |
| CN204138504U (en) | Garbage leachate treatment device | |
| CN108017160B (en) | Pressurized fluidized biological sewage and wastewater treatment device | |
| CN202046977U (en) | Anaerobic-aerobic integrated reactor | |
| CN205061690U (en) | Anaerobism - good oxygen integrative sewage treatment device | |
| MD4382C1 (en) | Combined biogas-production reactor | |
| CN102992480A (en) | Device and process for carrying out autotrophic denitrification treatment on nitrate nitrogen in sewage based on non-foaming hydrogen supply | |
| CN207002512U (en) | A kind of New-type refuse vehicle percolation liquid treating system | |
| CN218146280U (en) | Low-power-consumption facility suitable for treating rural domestic sewage | |
| CN206814483U (en) | Integrated livestock and poultry cultivating wastewater purification device | |
| CN210974071U (en) | Water seal device of anaerobic tank | |
| CN102515340A (en) | Upper-flow sequencing batch methane tank | |
| CN107381937A (en) | A kind of livestock breeding wastewater handling process system | |
| CN101445296A (en) | Apparatus for biologically treating livestock and poultry waster water | |
| CN203048669U (en) | Experimental auxiliary device of up-flow biogas digester | |
| CN206173163U (en) | Wastewater treatment device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| KA4A | Patent for invention lapsed due to non-payment of fees (with right of restoration) | ||
| MM4A | Patent for invention definitely lapsed due to non-payment of fees |