CN2791027Y - Three-phase biological fluidized bed reactor for sewage treatment - Google Patents
Three-phase biological fluidized bed reactor for sewage treatment Download PDFInfo
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- CN2791027Y CN2791027Y CN 200520030608 CN200520030608U CN2791027Y CN 2791027 Y CN2791027 Y CN 2791027Y CN 200520030608 CN200520030608 CN 200520030608 CN 200520030608 U CN200520030608 U CN 200520030608U CN 2791027 Y CN2791027 Y CN 2791027Y
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Abstract
The utility model discloses a gas-liquid-solid three-phase biological fluidized bed reactor for sewage treatment, which is used for solving the problems of complicated structure, auxiliary devices in a large quantity, large ground occupation, etc. existing in the present three-phase biological fluidized bed sewage treatment devices. At least one lifting pipe (2) is arranged in the axial direction in a barrel body of the reactor of the utility model, an outlet arranged at the top part of the lifting pipe (2) is extended into a diversion barrel (11) arranged in a barrel body (52) of a separation area, and a gas-liquid-solid separator (6) is arranged above the outlet arranged at the top part of the lifting pipe (2). The reactor is provided with a gas inlet pipe (10), and an outlet of the gas inlet pipe (10) is extended into the lifting pipe (2) through an inlet arranged at the bottom part of the lifting pipe (2). A water inlet (7) is arranged on the side wall of a barrel body (51) of a fluidized area. The utility model is mainly used for treating sewage in the petrochemical industry.
Description
Technical field
The utility model relates to a kind of gas-liquid-solid three-phase biological fluidized-bed reactor that is used for sewage disposal.
Background technology
Old three covers are adopted in the sewage disposal of petroleum chemical industry refinery at present mostly, first oil removal, flotation again, back aeration, sewage qualified discharge.But along with being in full swing of present China water-saving engineering, the consumption that reduces crude oil fresh water per ton has become one of refinery urgent problem.The fresh water consumption amount that external refinery advanced level is processed crude oil per ton is generally less than 0.5 ton, and domestic mean level (ML) is 2.4 tons.Aspect sewage discharge, the quantity of wastewater effluent that external advanced level is processed crude oil per ton is 0.2 ton, and domestic mean level (ML) is 1.78 tons.Therefore, under the situation that China's water resources is deficient day by day at present, realize reusing sewage, reduce quantity of wastewater effluent, save the fresh water consumption, reduce processing costs, just seem particularly important.
Handle the present Research of petrochemical effluent from domestic and international biochemical process, the present mainly mechanism and the kinetics thereof of toxic substance in free bacterium degradation of sewage, and the biochemical process feasibility of disposing of sewage, some theories and cut-and-try work have been done in aspect such as decontamination effect improving and operating procedure thereof, but during biochemical process disposed of sewage such as how further adopting modern biotechnology and means to strengthen the biological activity and the processing power of microorganism species, how further to reduce the reaction volume of bio-reactor, and how further to improve and problems such as processing power that strengthens bio-reactor and efficient, all lack necessary further investigation.The three-phase fluidized bed biological treatment device of industry sewage disposals such as Chinese patent z187102232 (authorization number for CNl008727B) has proposed a kind ofly to be used to refine oil, chemical industry has characteristics such as processing efficiency height, reflux ratio are low; Its shortcoming is that structure is very complicated, required auxiliary facility also more (such as demoulding device, spray equipment etc.), and output investment ratio is bigger.The gas that z194231726 (Granted publication number be CN2209673Y) proposes promotes the multi-joint fluidized-bed reaction of three-phase pond, is to add riser tube in Da Chi, and its principle is close with the three-phase fluidized bed principle; Shortcoming is that floor space is big, investment is high, only is fit to the transformation of original waste disposal plant.
Summary of the invention
Technical problem to be solved in the utility model is: the existing complex structure of existing three-phase biologic fluidized-bed waste disposal plant, problem such as auxiliary facility is more, floor space is big.
For addressing the above problem, the technical solution adopted in the utility model is: a kind of three-phase biological fluidized bed reactor that is used for sewage disposal, comprise a reactor shell, the top of reactor shell is the disengaging zone cylindrical shell, the bottom is the fluidization regions cylindrical shell, be provided with guide shell in the cylindrical shell of disengaging zone, it is characterized in that: be provided with 1 riser tube in the reactor shell vertically at least, the outlet at riser tube top stretches in the guide shell, the top of riser tube top exit is provided with gas-liquid-solid separator, reactor is provided with inlet pipe, and the outlet of inlet pipe is stretched in the riser tube by the inlet of riser tube bottom, and the sidewall of fluidization regions cylindrical shell is provided with water-in.
Adopt the utility model, have following beneficial effect: the utility model has solved existing three-phase biologic fluidized-bed waste disposal plant complex structure, floor space is wide, equipment is huge problem; Can obviously reduce the sewage disposal expense, increase economic efficiency.The utility model adopts inside to dose carrier, body-internal-circulation in operating process, to improve microorganism and activated sludge concentration, shortens the reaction times, thereby can improve the clearance of substrate in the unit time.The utility model adopts riser tube lifting, body-internal-circulation formula fluidized-bed, has following characteristics: sludge activity and microorganism concn height in (1) fluidized-bed, and microorganism concn is generally 12～40 grams per liters, average out to 20 grams per liters; (2) equipment is simple, and less investment can be saved the mud return-flow system; (3) the bottom aeration is a fluidized wind, also is the oxygen source of mud and microorganism; (4) sludge output is few, and sewage disposal mainly relies on microbial film; (5) effluent quality is good, can reach the industrial cycle water quality standard through secondary sedimentation.
In the operating process, violent because of the turbulence of riser tube inner fluid, can slough aging blocked up microbial film on the carrier voluntarily, active sludge in the fluidized-bed can self circulate and save the activity sludge reflux system like this, also saved external demoulding device, made mud increase age, sludge discharge reduces.In addition, oxygen source and propulsion source can be shared, and the required power consumption of fluidized-bed is few; Device is simple, and not strict to the degree of uniformity requirement of water distribution, gas distribution, the industrialization feasibility is good.The utility model is provided with gas-liquid-solid separator above the riser tube top exit, can carry out the solid separation of gas-liquid effectively.Riser tube can be provided with many, and its advantage is: (1) can reduce the height of equipment effectively, makes it not limited greater than 10 ratio by the fluidized-bed aspect ratio; (2) gas distribution is more even, and the gas, liquid, solid contact mass transfer is more effective; (3) can reduce power consumption, save energy consumption.
The utility model is used to handle the sewage of petroleum chemical industry, the multiple pollutent of sewage can be reduced to simultaneously the scope of national Specification.
The utility model is described in more detail below in conjunction with the drawings and specific embodiments.
Description of drawings
Fig. 1 is the utility model reactor sectional view vertically, and reactor is provided with 1 riser tube, and gas-liquid-solid separator is a cone surface shape.
Fig. 2 is the synoptic diagram of plate shaped gas-liquid-solid separator.
Fig. 3 is the synoptic diagram of rounding cone-shaped gas-liquid-solid separator.
The synoptic diagram of the gas-liquid-solid separator that Fig. 4 is made up of a cone and inverted cone.
Fig. 5 is the sectional view that its fluidization regions cylindrical shell cross section of reactor of 7 riser tubes is set.
Embodiment
Referring to Fig. 1, the gas-liquid-solid three-phase biological fluidized-bed reactor (abbreviating reactor as) that the utility model is used for sewage disposal comprises a reactor shell, the top of reactor shell is the columnar disengaging zone cylindrical shell 52 of hole enlargement, the bottom is columnar fluidization regions cylindrical shell 51, links to each other with an inverted cone section between disengaging zone cylindrical shell 52 and the fluidization regions cylindrical shell 51.Be provided with a co-axial with it guide shell 11 in the disengaging zone cylindrical shell 52, guide shell 11 is a cylindrical drum, and its underpart is the cylindrical shell of the shape of falling the frusto-conical face of undergauge structure.The negative area 1 of looping between the inwall of the outer wall of guide shell 11 and disengaging zone cylindrical shell 52.Leave annulus 13 between the bottom of guide shell 11 and the reactor shell inverted cone section, obviously this annulus 13 is positioned at the bottom of negative area 1.
Be provided with 1 riser tube 2 in the reactor shell vertically, riser tube 2 has a top exit and bottom inlet, and the outlet at its top stretches in the guide shell 11.The top of riser tube 2 top exits is provided with a gas-liquid-solid separator 6.Gas-liquid-solid separator 6 shown in Figure 1 is a cone surface shape; Gas-liquid-solid separator 6 can also adopt as Fig. 2, Fig. 3 or form shown in Figure 4.Gas-liquid-solid separator 6 can adopt various methods commonly used and parts to be fixed on the riser tube 2.Form annulus 14 between gas-liquid-solid separator 6 and riser tube 2 top exits.As shown in Figure 1, reactor is provided with 1 inlet pipe 10, and inlet pipe 10 enters reactor by the bottom bulkhead of reactor shell, and its outlet is stretched in the riser tube 2 by the bottom inlet of riser tube 2.Reactor of the present utility model, riser tube 2 are provided with 1 at least, reactor setting shown in Figure 1 be 1.Reactor shown in Figure 5, setting be 7 riser tubes 2.Under the bigger situation of treatment capacity, many riser tubes (can be provided with tens of, for example 80) can be set.When many riser tubes 2 were set, each root riser tube 2 was provided with in reactor shell vertically, and the outlet at riser tube 2 tops all stretches in the guide shell 11, and the top of each root riser tube 2 top exit is respectively equipped with a gas-liquid-solid separator 6.Reactor is provided with the inlet pipe 10 identical with riser tube 2 quantity, and the outlet of each root inlet pipe 10 is stretched in the riser tube 2 by the inlet of each root riser tube 2 bottom respectively.
As shown in Figure 1, be provided with effluent trough 4 around the outer wall of disengaging zone cylindrical shell 52, the bottom of effluent trough 4 is provided with water outlet 8.Be provided with water port 12 on negative area 1 between the inwall of the outer wall of guide shell 11 and disengaging zone cylindrical shell 52 and the disengaging zone cylindrical shell 52 between the effluent trough 4, water port 12 is communicated with negative area 1 with effluent trough 4.The sidewall of fluidization regions cylindrical shell 51 is provided with water-in 7, and water-in 7 can be located at the top or the bottom of fluidization regions cylindrical shell 51.The bottom bulkhead of reactor shell also is provided with drain 9, the usefulness of blowdown during for shut-down.
The operating process of reactor shown in Figure 1 is such: sewage enters annular space between the inwall of the outer wall of riser tube 2 and fluidization regions cylindrical shell 51 flow downward (in operating process, forming gas-liquid-solid three-phase fluid bed 3 in this annular space) from water-in 7.Carrier and high reactivity mud are housed in the reactor, and the carrier surface growth has microbial film.Carrier can adopt gac, and its particle diameter is 1～2.5 millimeter, and density is 995 kilograms per cubic meter.Feed gas (pressurized air) through inlet pipe 10 to the bottom of riser tube 2.Gas is sent into riser tube 2 with carrier by the bottom inlet of riser tube 2 with sewage as propulsion source, and the turbulence mixing is upwards flowed in riser tube 2, is flowed out by the top exit and the annulus between the gas-liquid-solid separator 6 14 of riser tube 2 again.After the centrifugation of gas-liquid-solid separator 6, all carriers and portion water, gas and active sludge circulate downwards along the annular space that forms between the inwall of the outer wall of riser tube 2 and guide shell 11, fluidization regions cylindrical shell 51, continue to get back to riser tube 2 through the bottom inlet of riser tube 2.Part active sludge after gas-liquid-solid separator 6 separates and water and portion gas guide shell 11 in on mobile, gas is released and upwards flows and enters atmosphere in this process, and active sludge and water enter negative area 1 through guide shell 11 top overflows and carries out sedimentation.After mud, water separate in negative area 1, the fluidized-bed 3 in the annular space between the inwall of the outer wall of active sludge through passing back into riser tube 2 and fluidization regions cylindrical shell 51 in the annulus 13 of 1 bottom, negative area, continuation circulates downwards.1 the top in the negative area, the water after the processing enters effluent trough 4 through water port 12, and the water in the effluent trough 4 is then through water outlet 8 outflow reactors of its bottom.Above-mentioned operating process is that circulation is carried out continuously; In operating process, formation gas-liquid-solid three-phase biological fluidized bed 3 in the annular space in the riser tube 2, between the inwall of the outer wall of riser tube 2 and guide shell 11 and fluidization regions cylindrical shell 51 from bottom inlet to the space between the top exit.The distribution of fluidized-bed 3 on fluidization regions cylindrical shell 51 cross sections when Fig. 5 shows reactor 7 riser tubes 2 are set; Fluidized-bed 3 in each root riser tube 2 from bottom inlet to the space between the top exit, and in the space that inwall constituted by outer wall, guide shell 11 and the fluidization regions cylindrical shell 51 of each root riser tube 2.The operating process and the reactor that 1 riser tube 2 is set shown in Figure 1 of reactor that many riser tubes 2 are set is similar, and explanation is omitted.
Three-phase biological fluidized bed reactor of the present utility model (referring to Fig. 1) can not set out tank 4 (also just not offering water port 12 on disengaging zone cylindrical shell 52).Can adopt this moment various methods commonly used or device (for example adopting pipeline) that the water after handling in the negative area 1 is drawn reactor.The cylindrical shell of the shape of falling the frusto-conical face of undergauge structure can not adopted in the bottom of guide shell 11, and this moment, guide shell 11 was single cylindrical drum structure, still left annulus 13 between its bottom and the reactor shell inverted cone section.
Among the utility model Fig. 2 to Fig. 5, the represented technical characterictic of all unaccounted Reference numerals all with Fig. 1 in identical.Among Fig. 1, represent the flow direction of gas, liquid, solid or gas-liquid-solid mixture with arrow.
The riser tube 2 and the gas-liquid-solid separator 6 of the utility model reactor can adopt stainless material, and remaining parts can adopt the carbon steel material that is coated with corrosion protection coating.
The utility model reactor is mainly used in the sewage of handling petroleum chemical industry, and its treatment capacity can design as required.Effluent index can reach:
COD
Cr≤ 50 mg/litre;
BOD
5≤ 20～30 mg/litre;
SS≤15 mg/litre;
NH
3-N≤5 mg/litre.
Wherein, COD
CrBe chemical oxygen demand (potassium dichromate process), BOD
5Be five-day BOD, SS is a suspended substance, NH
3-N is an ammonia nitrogen.
Claims (2)
1, a kind of three-phase biological fluidized bed reactor that is used for sewage disposal, comprise a reactor shell, the top of reactor shell is disengaging zone cylindrical shell (52), the bottom is fluidization regions cylindrical shell (51), be provided with guide shell (11) in the disengaging zone cylindrical shell (52), it is characterized in that: be provided with 1 riser tube (2) in the reactor shell vertically at least, the outlet at riser tube (2) top stretches in the guide shell (11), the top of riser tube (2) top exit is provided with gas-liquid-solid separator (6), reactor is provided with inlet pipe (10), the outlet of inlet pipe (10) is stretched in the riser tube (2) by the inlet of riser tube (2) bottom, and the sidewall of fluidization regions cylindrical shell (51) is provided with water-in (7).
2, three-phase biological fluidized bed reactor according to claim 1, it is characterized in that: the outer wall around disengaging zone cylindrical shell (52) is provided with effluent trough (4), the bottom of effluent trough (4) is provided with water outlet (8), is provided with water port (12) on negative area (1) between the inwall of the outer wall of guide shell (11) and disengaging zone cylindrical shell (52) and the disengaging zone cylindrical shell (52) between the effluent trough (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200520030608 CN2791027Y (en) | 2005-04-28 | 2005-04-28 | Three-phase biological fluidized bed reactor for sewage treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200520030608 CN2791027Y (en) | 2005-04-28 | 2005-04-28 | Three-phase biological fluidized bed reactor for sewage treatment |
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| Publication Number | Publication Date |
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| CN2791027Y true CN2791027Y (en) | 2006-06-28 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 200520030608 Expired - Lifetime CN2791027Y (en) | 2005-04-28 | 2005-04-28 | Three-phase biological fluidized bed reactor for sewage treatment |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101781016A (en) * | 2010-03-04 | 2010-07-21 | 陕西科技大学 | Three-phase biological fluidized bed |
| CN103663690A (en) * | 2012-09-10 | 2014-03-26 | 中国石油化工集团公司 | Sewage treatment bioreactor |
| CN105457461A (en) * | 2015-12-29 | 2016-04-06 | 原初科技（北京）有限公司 | Carbon dioxide absorption and mineralization device and method |
| WO2018076962A1 (en) * | 2016-10-26 | 2018-05-03 | 中国科学院青岛生物能源与过程研究所 | Internal loop reactor having both reaction and separation functions |
-
2005
- 2005-04-28 CN CN 200520030608 patent/CN2791027Y/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101781016A (en) * | 2010-03-04 | 2010-07-21 | 陕西科技大学 | Three-phase biological fluidized bed |
| CN103663690A (en) * | 2012-09-10 | 2014-03-26 | 中国石油化工集团公司 | Sewage treatment bioreactor |
| CN103663690B (en) * | 2012-09-10 | 2015-05-13 | 中国石油化工集团公司 | Sewage treatment bioreactor |
| CN105457461A (en) * | 2015-12-29 | 2016-04-06 | 原初科技（北京）有限公司 | Carbon dioxide absorption and mineralization device and method |
| CN105457461B (en) * | 2015-12-29 | 2018-04-10 | 原初科技（北京）有限公司 | A kind of carbon dioxide absorption and the device and method that mineralizes |
| US10343113B2 (en) | 2015-12-29 | 2019-07-09 | Yuanchu Technology (Beijing) Co., Ltd. | Apparatus and method for absorbing and mineralizing carbon dioxide |
| WO2018076962A1 (en) * | 2016-10-26 | 2018-05-03 | 中国科学院青岛生物能源与过程研究所 | Internal loop reactor having both reaction and separation functions |
| US10376855B2 (en) | 2016-10-26 | 2019-08-13 | Qingdao Institute Of Bioenergy And Bioprocess Technology, Chinese Academy Of Science | Internal loop airlift reactor for process intensification integrating reaction and separation |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |
Expiration termination date: 20150428 Granted publication date: 20060628 |