CN110217948B - Guide shell circulation reactor - Google Patents
Guide shell circulation reactor Download PDFInfo
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- CN110217948B CN110217948B CN201910620141.6A CN201910620141A CN110217948B CN 110217948 B CN110217948 B CN 110217948B CN 201910620141 A CN201910620141 A CN 201910620141A CN 110217948 B CN110217948 B CN 110217948B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 189
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- 239000012528 membrane Substances 0.000 claims abstract description 38
- 238000005273 aeration Methods 0.000 claims abstract description 23
- 239000012530 fluid Substances 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims description 24
- 238000011001 backwashing Methods 0.000 claims description 17
- 239000012510 hollow fiber Substances 0.000 claims description 17
- 239000011550 stock solution Substances 0.000 claims description 17
- 150000003839 salts Chemical class 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 9
- 230000005514 two-phase flow Effects 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 7
- 235000015097 nutrients Nutrition 0.000 claims description 7
- 230000000050 nutritive effect Effects 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 3
- 238000004364 calculation method Methods 0.000 claims description 2
- 238000001514 detection method Methods 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 230000011218 segmentation Effects 0.000 claims 1
- LPUQAYUQRXPFSQ-DFWYDOINSA-M monosodium L-glutamate Chemical compound [Na+].[O-]C(=O)[C@@H](N)CCC(O)=O LPUQAYUQRXPFSQ-DFWYDOINSA-M 0.000 abstract description 7
- 235000013923 monosodium glutamate Nutrition 0.000 abstract description 7
- 239000004223 monosodium glutamate Substances 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 5
- 239000010842 industrial wastewater Substances 0.000 abstract description 4
- 238000004065 wastewater treatment Methods 0.000 abstract description 3
- 239000010865 sewage Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 20
- 238000011010 flushing procedure Methods 0.000 description 9
- 238000007789 sealing Methods 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 6
- 238000009826 distribution Methods 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 2
- AKVPUSMVWHWDGW-UHFFFAOYSA-N [C].[N].[P] Chemical compound [C].[N].[P] AKVPUSMVWHWDGW-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 235000019698 starch Nutrition 0.000 description 2
- 239000008107 starch Substances 0.000 description 2
- WHUUTDBJXJRKMK-UHFFFAOYSA-N Glutamic acid Natural products OC(=O)C(N)CCC(O)=O WHUUTDBJXJRKMK-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 235000013922 glutamic acid Nutrition 0.000 description 1
- 239000004220 glutamic acid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 235000013379 molasses Nutrition 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009966 trimming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/04—Oxidation reduction potential [ORP]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C02F2209/11—Turbidity
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- C02F2209/22—O2
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/42—Liquid level
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- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C02F2305/06—Nutrients for stimulating the growth of microorganisms
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
The invention discloses a draft tube loop reactor, and relates to an integrated multistage series connection two-stage conical draft tube reactor sewage treatment device applied to monosodium glutamate industrial wastewater treatment, which comprises a PLC automatic control system, and a three-point water inlet system, a pulse type aeration system, a multistage series connection draft tube reaction device and a membrane interception water outlet system which are respectively connected with the PLC automatic control system, wherein the three-point water inlet system is connected with the multistage series connection draft tube reaction device through a pipeline, the bottom of the multistage series connection draft tube reaction device is connected with the pulse type aeration system through a pipeline, and one side of the multistage series connection draft tube reaction device is connected with the membrane interception water outlet system through a pipeline; small floor area, low gas consumption, good fluid state condition and strong treatment effect.
Description
Technical Field
The invention belongs to the technical field of industrial wastewater treatment, and particularly relates to an integrated multistage series connection two-stage conical draft tube reactor sewage treatment device applied to monosodium glutamate industrial wastewater treatment.
Background
China is a big country for producing monosodium glutamate, the capacity of the monosodium glutamate industry in 2015 China accounts for 75% of the world, the supply amount accounts for more than 60% of the world, the monosodium glutamate production generally takes rice, starch and molasses as main raw materials, glutamic acid is extracted by fermentation and then refined into monosodium glutamate, and a large amount of industrial wastewater is generated in the refining process. The wastewater is characterized in that the Chemical Oxygen Demand (COD) and the total nitrogen content (TN) are higher and can reach 1500mg/L and 150mg/L, and the wastewater is difficult to reach the first-grade A discharge standard of GB8978-2002 by treatment.
The existing circulating reactor is mainly researched from characteristic parameters such as internal gas content, circulating liquid velocity, mass transfer coefficient and the like of the circulating reactor to improve mass transfer and heat transfer effects of the circulating reactor, but has a plurality of influence factors such as pressure, apparent gas velocity, liquid phase physical properties, shape and size of the reactor, and a guide cylinder is used as an internal key part and has great influence on gas-liquid distribution effect and mass transfer efficiency of the circulating reactor. In the utility model patent with publication number CN208292824U, a biochemical strengthening treatment system for starch monosodium glutamate wastewater is disclosed, the water quality after the treatment of the system can reach the first-level standard in the integrated wastewater discharge standard GB 208292824U-1996, but the anoxic tank is provided with two submersible stirrers, the anoxic tank is totally closed, the stirrers are difficult to maintain when having problems, the occupied area is large, and the number of parts needing manual operation is large in the operation process. In the invention patent with publication number CN106904791A, the flow field distribution of the part of the aeration oxidation tank is not good, and if the aeration intensity is to be ensured, a large amount of gas supply is needed, which wastes energy.
Disclosure of Invention
In order to solve the defects in the prior art, the invention provides the guide shell circulation reactor which is small in occupied area, small in air consumption, good in fluid state condition and strong in treatment effect.
The technical scheme adopted by the invention for solving the technical problem is as follows: a draft tube circulation reactor comprises a PLC automatic control system, and a three-point water inlet system, a pulse type aeration system, a multi-stage series draft tube reaction device and a membrane interception water outlet system which are respectively connected with the PLC automatic control system, wherein the three-point water inlet system is connected with the multi-stage series draft tube reaction device through a pipeline, the bottom of the multi-stage series draft tube reaction device is connected with the pulse type aeration system through a pipeline, and one side of the multi-stage series draft tube reaction device is connected with the membrane interception water outlet system through a pipeline.
Further, the three-point water inlet system comprises a water inlet tank, the top of the water inlet tank is connected with a nutritive salt adding device, one end of the top of the water inlet tank is provided with a stock solution inlet, the stock solution inlet is provided with a stock solution inlet control valve, one side of the water inlet tank is provided with a water outlet a, and the water outlet is connected with the multistage series connection guide cylinder reaction device through a pipeline.
Further, the multistage series draft tube reaction device comprises an outer tube, a plurality of bipolar conical inner tubes which are sequentially connected are arranged in the outer tube, a water inlet a is formed in one side of the outer tube, a water outlet b is formed in the other side of the outer tube, a plurality of air inlets are formed in the bottom of the outer tube, and the plurality of air inlets are connected to the pulse type aeration system through pipelines; the water inlet a is connected with the water outlet a of the three-point water inlet system through a pipeline, and the water outlet b is connected with the membrane interception water outlet system through a pipeline.
Furthermore, the pulse type aeration system comprises a plurality of pulse generation devices which are connected in sequence, one side of each pulse generation device is connected with an air compressor, the number of the pulse generation devices is consistent with that of air inlets of the multistage series connection guide cylinder reaction devices, and the pulse generation devices are connected with the air inlets of the multistage series connection guide cylinder reaction devices in a one-to-one correspondence manner.
Further, the membrane interception water outlet system comprises a hollow fiber membrane component, the bottom end of the hollow fiber membrane component is connected with a water outlet b of the multistage series draft tube reaction device through a pipeline, a raw water pump and a security filter are arranged on a connecting pipeline between the bottom end of the hollow fiber membrane component and the water outlet b, and the connecting pipeline is also connected with an air compressor through an air inlet valve; the top end of the hollow fiber membrane component is connected with a backwashing water tank through a pipeline.
Furthermore, the PLC automatic control system comprises a PLC automatic control box, a computer and a sensor, wherein the computer and the sensor are connected with the PLC automatic control box; the sensor comprises liquid level control sensors respectively arranged in the water inlet tank and the backwashing water tank, and a sensor group respectively arranged in each inner cylinder, wherein the sensor group comprises a temperature sensor, a DO sensor, a pH sensor and an ORP sensor.
The invention has the beneficial effects that: the energy consumption is low, and mass transfer efficiency is high, realizes the circulation flow under the impetus of density difference and gravity, has stirred tank and bubbling bed's function, does not have rotating parts, phase distribution is even, flash mixed, compares with traditional device, can bear higher COD concentration of intaking or the load of intaking, improves gas-liquid distribution effect, improves the gas content by a wide margin, and the fluid flow state condition is good, and compact structure, area is little to reduce cost, application prospect is extensive.
Drawings
FIG. 1 is a flow chart of the overall structure of the present invention;
FIG. 2 is a schematic view of the overall structure of the present invention;
FIG. 3 is a schematic view of a connection structure between a three-point water inlet system and a PLC automatic control system according to the present invention;
FIG. 4 is a schematic structural view of a multi-stage series draft tube reactor according to the present invention;
FIG. 5 is a schematic diagram of a pulse aeration system according to the present invention;
FIG. 6 is a schematic view of the connection structure of the membrane-trapped water outlet system and the multi-stage series draft tube reaction device according to the present invention;
fig. 7 is a schematic structural diagram of the PLC automatic control system of the present invention.
The reference numbers in the figures are as follows: 1. a three-point water inlet system, 2, a multi-stage series draft tube reaction device, 3, a pulse type aeration system, 4, a membrane interception water outlet system, 5, a PLC automatic control system, 1-1, a water inlet tank, 1-2, a stock solution inlet, 1-3, a stock solution inlet control valve, 1-4, a water outlet a, 1-5, a storage bin, 1-6, a batcher, 1-7, a stirring motor, 1-8, a stirrer, 1-9, a water inlet pump, 1-10, an electromagnetic valve, 1-11, a flowmeter a, 2-1, an outer cylinder, 2-2-1, a first-stage draft tube inner cylinder, 2-2, a second-stage draft tube inner cylinder, 2-2-3, a third-stage draft tube, 2-2, a two-stage conical inner cylinder, 2-3, a water inlet a, 2-4, a membrane interception water outlet system, 5, a PLC automatic control system, 1-1, 1-9, 1-2, 1, 2-2-2, 2-2-2, Water outlet b, 2-5, gas distributor, 2-6, water inlet b, 2-7, water inlet c, 2-8, gas outlet, 2-9, gas inlet a, 2-10, gas inlet b, 2-11, gas inlet c, 3-1, air compressor, 3-2, support leg, 3-3, collecting cover, 3-4, external connecting plate, 3-5, water sealing cover, 3-6, pulse generator, 3-6-1, straight cylinder, 3-7, internal connecting plate, 3-8, air valve, 3-9, air inlet pipe, 3-10, water sealing bucket, 3-11, air inlet control valve, 4-1, hollow fiber membrane module, 4-2, raw water pump, 4-3, security filter, 4-4, air inlet valve, 4-5 parts of an air compressor, 4-6 parts of a backwashing water tank, 4-7 parts of a water inlet valve, 4-8 parts of a pressure gauge, 4-9 parts of a lower discharge valve, 4-10 parts of a water outlet pipeline, 4-11 parts of a backwashing pipeline, 4-12 parts of a backwashing inlet, 4-13 parts of a flowmeter b, 4-14 parts of a ripple valve, 4-15 parts of a water outlet valve, 4-16 parts of a backwashing valve, 4-17 parts of a dosing valve, 4-18 parts of an outlet valve, 4-19 parts of an upper discharge valve, 5-1 part of a PLC automatic control box, 5-2 parts of a computer, 5-3 parts of a liquid level control sensor, 5-4 parts of a sensor group.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings and specific embodiments.
Example 1
As shown in fig. 1 and fig. 2, a draft tube loop reactor comprises a PLC automatic control system 5, and a three-point water inlet system 1, a pulse type aeration system 3, a multi-stage series draft tube reactor 2 and a membrane interception water outlet system 4 which are respectively connected with the PLC automatic control system 5, wherein the three-point water inlet system 1 is connected with the multi-stage series draft tube reactor 2 through a pipeline, the bottom of the multi-stage series draft tube reactor 2 is connected with the pulse type aeration system 3 through a pipeline, and one side of the multi-stage series draft tube reactor 2 is connected with the membrane interception water outlet system 4 through a pipeline.
As shown in fig. 7, the PLC automatic control system 5 includes a PLC automatic control box 5-1, a computer 5-2 and a sensor, and both the computer 5-2 and the sensor are connected to the PLC automatic control box 5-1; the sensors include a plurality of level control sensors 5-3 and a plurality of sensor groups 5-4, the sensor groups 5-4 including a temperature sensor, a DO sensor, a pH sensor, and an ORP sensor. The preferred PLC automatic control system 5 of this embodiment has an adaptive fuzzy controller, which can calculate and integrate the trimming parameters according to the real-time monitored data, and combine the conventional control algorithm and the fuzzy control algorithm to realize the optimal adjustment of the parameters. All pumps, valves, pressure gauges, flow meters and nutrient salt feeding devices in the reactor are connected with a PLC automatic control system 5.
As shown in fig. 3, the three-point water inlet system 1 comprises a water inlet tank 1-1, the top of the water inlet tank 1-1 is connected with a nutrient salt adding device, one end of the top of the water inlet tank 1-1 is provided with a stock solution inlet 1-2, the stock solution inlet is provided with a stock solution inlet control valve 1-3, one side of the water inlet tank 1-1 is provided with a water outlet a1-4, and the stock solution inlet 1-2 and the water outlet a1-4 are respectively located at two opposite sides of the water inlet tank 1-1; the nutritive salt adding device comprises a plurality of storage bins 1-5 which are sequentially connected, wherein each storage bin 1-5 is connected to the top of a water inlet tank 1-1 through a batcher 1-6, the nutritive salt adding device also comprises a stirring motor 1-7 which is installed on the top of the water inlet tank 1-1, one end of the stirring motor 1-7 is connected with a stirrer 1-8, and the stirrer 1-8 extends into the water inlet tank 1-1; the water outlet a1-4 is connected with the multistage series draft tube reaction device 2 through a pipeline, and a water inlet pump 1-9, an electromagnetic valve 1-10 and a flowmeter a1-11 are sequentially arranged on the connecting pipeline; a liquid level control sensor 5-3 is arranged in the water inlet tank 1-1, and the tops of the multiple storage bins 1-5 are connected to a PLC automatic control box 5-1 through lines.
The working process of the three-point water inlet system 1 is as follows: opening a stock solution inlet control valve 1-3, enabling raw water to enter a water inlet tank 1-1 from a stock solution inlet 1-2, uploading detected data to a PLC automatic control box 5-1 by a liquid level control sensor 5-3, transmitting the data to a computer 5-2 by the PLC automatic control box 5-1 for integrated calculation, further controlling a storage bin 1-5 to feed nutrient salt into the water inlet tank 1-1 through a batcher 1-6, driving a stirrer 1-8 by a stirring motor 1-7 to stir the raw water in the water inlet tank, enabling the pretreated raw water to flow out through a water outlet a1-4, and enabling the pretreated raw water to enter a multistage series draft tube reaction device 2 after passing through a water inlet pump 1-9, an electromagnetic valve 1-10 and a flow meter a 1-11. The nutrient salt feeding device of the three-point water inlet system 1 is mainly used for maintaining the carbon nitrogen phosphorus ratio C: N: P of wastewater to be 100:5:1, the batchers 1-6 realize accurate feeding of materials, the utilization rate of nutrient salts is improved, and the PLC automatic control system controls valves, the flow meter a1-11 and related elements. The three-point water inlet system 1 reduces the head loss of unit time, improves the efficiency, and can automatically adjust the carbon nitrogen phosphorus ratio of the wastewater.
As shown in fig. 4, the multistage series draft tube reactor 2 comprises an outer tube 2-1, and the preferred size of the outer tube 2-1 in this embodiment is: the length of the inner cylinder 2-2 is 3600mm, the width of the inner cylinder 2-2 is 1200mm, the height of the inner cylinder 2-2 is 4600mm, a plurality of two-pole conical inner cylinders 2-2 connected in sequence are arranged in the outer cylinder 2-1, the number of the two-pole conical inner cylinders 2-2 preferred in the embodiment is three, the three two-pole conical inner cylinders 2-2 are respectively the first-stage guide cylinder inner cylinder 2-2-1, the second-stage guide cylinder inner cylinder 2-2-2 and the third-stage guide cylinder 2-2-3, the heights of the first-stage guide cylinder inner cylinder 2-2-1, the second-stage guide cylinder inner cylinder 2-2-2 and the third-stage guide cylinder 2-2-3 are different and are arranged in sequence from high to low, the height of the first-stage guide cylinder inner cylinder 2-2-1 is 4200mm, the height of the second-stage guide cylinder inner cylinder 2-2-2 is 3600mm, the height of the third-2-3 is 2400mm, the two-pole conical inner barrel 2-2 is conical, and the preferred conicity is 1: 0.35 at 2-2 height of the two-pole conical inner cylinder
The section is arranged, and the section interval is 40mm, so that the distribution of an internal flow field is improved; and gas distributors 2-5 are arranged below the three two-pole conical inner cylinders 2-2, the distance between the gas distributors 2-5 and the two-pole conical inner cylinders 2-2 is 50mm, and the three gas distributors 2-5 respectively convey gas into the first-stage guide cylinder inner cylinder 2-2-1, the second-stage guide cylinder inner cylinder 2-2-2 and the third-stage guide cylinder 2-2-3. A water inlet a2-3 is arranged on one side of the outer cylinder 2-1, a water outlet b2-4 is arranged on the other side of the outer cylinder 2-1, a water inlet b2-6, a water inlet c2-7 and an air outlet 2-8 are arranged at the top of the outer cylinder 2-1, the air outlet 2-8 is positioned between the water inlet b2-6 and the water inlet c2-7, an air inlet a2-9, an air inlet b2-10 and an air inlet c2-11 are arranged at the bottom of the outer cylinder 2-1, the air inlet a2-9 is positioned below the inner cylinder 2-2-1 of the primary guide cylinder, and the air inlet b2-10 is positioned at the secondary guide cylinderThe air inlet c2-11 is positioned below the third-stage flow guide inner cylinder 2-2-3 and below the cylinder inner cylinder 2-2-2; the water inlet a2-3 is connected with the water outlet a1-4 of the three-point water inlet system 1 through a pipeline, the water outlet b2-4 is connected with the membrane interception water outlet system 4 through a pipeline, and the air inlet a2-9, the air inlet b2-10 and the air inlet c2-11 are connected with the pulse type aeration system 3 through pipelines. The three two-pole conical inner cylinders 2-2 are internally provided with sensor groups 5-4.
The main body outer cylinder 2-1 of the multistage series draft tube reaction device 2 is a cuboid, the interior of the multistage series draft tube reaction device is divided into three reaction zones, namely three two-pole conical inner cylinders 2-2, and in the operation process, pretreated raw water is respectively fed into the reaction zones from a water inlet a2-3, a water inlet b2-6, a water inlet c2-7 and a water inlet ratio of 7: 2: 1 enters an outer barrel 2-1, gas enters a bipolar conical inner barrel 2-2 from a gas distributor 2-5 at the bottom, so that the gas phase content of the bipolar conical inner barrel 2-2 is far larger than that of the outer barrel 2-1, the density difference is formed between the inside and the outside of a guide barrel reaction device by fluid, the density difference forms the driving force of the integral circular flow in the guide barrel reaction device under the action of gravity, the mixed fluid with lower density in the bipolar conical inner barrel 2-2 flows upwards, the mixed fluid with higher density in an outer ring space flows downwards, and further the gas-liquid two-phase flow continuously flows upwards into the outer barrel 2-1 from the bipolar conical inner barrel 2-2 and then flows downwards into the bipolar conical inner barrel 2-2 from the outer barrel 2-1 to flow circularly. In the circulating flow process, the upper gas-liquid mixed fluid on the inner cylinder 2-2-1 of the first-stage guide cylinder overflows and flows to the inner cylinder 2-2-2 of the second-stage guide cylinder, similarly, the gas on the inner cylinder 2-2-2 of the second-stage guide cylinder enters from the bottom gas distributor 2-5, the gas-liquid two-phase flows in the inner cylinder of the same-stage guide cylinder, the upper gas-liquid mixed fluid overflows and flows to the inner cylinder 2-2-3 of the third-stage guide cylinder, the gas on the inner cylinder 2-2-3 of the third-stage guide cylinder enters from the bottom gas distributor 2-5, the gas-liquid two-phase flows in the inner cylinder of the same-stage guide cylinder, and finally flows out from the right water outlet b 2-4.
As shown in fig. 5, the pulse aeration system 3 comprises a plurality of pulse generating devices connected in sequence, one side of each pulse generating device is connected with an air compressor 3-1 through a pipeline, and an air inlet control valve 3-11 is arranged on a connecting pipeline between each pulse generating device and the air compressor 3-1; the number of the pulse generating devices preferred in this embodiment is three, and is the same as the number of the air inlets of the multistage series draft tube reaction device 2, and the pulse generating devices are connected with the air inlets of the multistage series draft tube reaction device 2 in a one-to-one correspondence manner through pipelines. The pulse generator comprises supporting legs 3-2, a collecting cover 3-3 is mounted at the top end of each supporting leg 3-2, an outer connecting plate 3-4 is arranged at the joint of each supporting leg 3-2 and the collecting cover 3-3, a water sealing cover 3-5 is arranged below each collecting cover 3-3, the water sealing cover 3-5 is connected with a straight cylinder 3-6-1 of the pulse generator 3-6, an inner connecting plate 3-7 is arranged at the joint of the water sealing cover 3-5 and the straight cylinder 3-6-1, and an air inlet pipe 3-9 is arranged at the bottom of the pulse generator 3-6; a water seal hopper 3-10 is formed among the outer wall of the pulse generator 3-6, the side wall of the water seal cover 3-5 and the inner wall of the supporting leg 3-2; the top of the collecting cover 3-3 is provided with an air valve 3-8, and the three air valves 3-8 of the pulse generating device are respectively connected with an air inlet a2-9, an air inlet b2-10 and an air inlet c2-11 of the multistage series guide shell reaction device 2 through pipelines.
The working flow of the pulse type aeration system 3 is as follows: the air in the air compressor 3-1 is supplied to the pulse generator 3-6 at a small flow rate through the air inlet pipe 3-9 and gathered in the water seal cover 3-5, the water level in the straight cylinder 3-6-1 is reduced along with the increase of the air, and when the water level is reduced to the lower edge of the water seal cover 3-5, the air in the water seal cover 3-5 rapidly bypasses the lower edge of the water seal cover 3-5 and enters the collection cover 3-3. When the compressed air rushes out of the water sealing cover 3-5, the water level in the straight cylinder 3-6-1 quickly rises to the top of the straight cylinder 3-6-1 and overflows out of the straight cylinder 3-6-1, the lower edge of the water sealing cover 3-5 is submerged, the water sealing cover 3-5 stops exhausting air, and when the pulse generator 3-6 is fully filled with air, the air is instantaneously and completely released into the multi-stage series guide cylinder reaction device 2. When the pulse type aeration system 3 operates, the external air supply to the pulse type aeration system 3 is continuous and low in strength, and the internal air supply of the pulse type aeration system 3 is intermittent and high in strength, so that the air supply amount is reduced and the energy is saved on the premise of ensuring the aeration strength.
As shown in fig. 6, the membrane-intercepting water-outlet system 4 comprises a hollow fiber membrane module 4-1, the bottom end of the hollow fiber membrane module 4-1 is connected with a water outlet b2-4 of the multistage series draft tube reaction device 2 through a pipeline, a raw water pump 4-2, a cartridge filter 4-3, a water inlet valve 4-7 and a pressure gauge 4-8 are arranged on a connecting pipeline between the bottom end of the hollow fiber membrane module 4-1 and the water outlet b2-4, and an air compressor 4-5 is further connected through an air inlet valve 4-4; one end of a connecting pipeline between the bottom end of the hollow fiber membrane component 4-1 and the water outlet b2-4 is connected with a drainage pipeline, and a lower drain valve 4-9 is arranged on the drainage pipeline; the top end of the hollow fiber membrane component 4-1 is connected with a water outlet pipeline 4-10, one end of the water outlet pipeline 4-10 extends into the backwashing water tank 4-6, the other end of the water outlet pipeline extends into the multi-stage series connection guide cylinder reaction device 2, the water outlet pipeline 4-10 is connected with one end of a backwashing pipeline 4-11, and the other end of the backwashing pipeline 4-11 is connected with a backwashing inlet 4-12 arranged at one side of the backwashing water tank 4-6; the joint of the hollow fiber membrane component 4-1 and the water outlet pipeline 4-10 is taken as a boundary point a, the joint of the backwashing pipeline 4-11 and the water outlet pipeline 4-10 is taken as a boundary point b, and one side of the boundary point a on the water outlet pipeline 4-10 is provided with a flowmeter b4-13, a wave water valve 4-14 and a pressure gauge 4-8; the other side of the dividing point a on the water outlet pipeline 4-10 is provided with a pressure gauge 4-8; one side of a dividing point b on the water outlet pipeline 4-10 is provided with a water outlet valve 4-15, a flow meter b4-13 and an outlet valve 4-18; and a backwashing valve 4-16, a flowmeter b4-13, a dosing valve 4-17, a cartridge filter 4-3 and a raw water pump 4-2 are sequentially arranged on the backwashing pipeline 4-11. The water outlet pipeline 4-10 is also connected with an upper discharge pipeline, and the upper discharge pipeline is provided with an upper discharge valve 4-19. And a liquid level control sensor 5-3 is arranged in the backwashing water tank 4-6.
The work flow of the membrane interception water outlet system 4 is as follows: the gas-liquid mixed fluid flowing out of the multistage series draft tube reaction device 2 flows into the hollow fiber membrane component 4-1 through the raw water pump 4-2, the cartridge filter 4-3, the water inlet valve 4-7 and the pressure gauge 4-8 to be filtered, then the hollow fiber membrane component 4-1 is back flushed, and then the forward flushing, the filtering, the back flushing and the forward flushing are carried out circularly. The forward flushing comprises flushing the surface of the membrane wire by liquid phase flow or gas-liquid two-phase flow, preferably flushing the surface of the membrane wire by gas-liquid two-phase flow when the raw water turbidity is 0-100NTU, and intermittently switching the wave water valves 4-14. When the turbidity of raw water is higher than 100NTU, on the basis of flushing the surface of the membrane wire by adopting gas-liquid two-phase flow, high-flow-rate liquid-phase flushing is carried out for one time after the cycles of filtering, backwashing and forward flushing. The system can effectively prevent the membrane filaments from breaking while ensuring the turbidity discharge performance of the membrane component.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered as the technical solutions and the inventive concepts of the present invention within the technical scope of the present invention.
Claims (4)
1. The draft tube loop reactor is characterized by comprising a PLC (programmable logic controller) automatic control system (5), and a three-point water inlet system (1), a pulse type aeration system (3), a multi-stage series draft tube reaction device (2) and a membrane interception water outlet system (4) which are respectively connected with the PLC automatic control system (5), wherein the three-point water inlet system (1) is connected with the multi-stage series draft tube reaction device (2) through a pipeline, the bottom of the multi-stage series draft tube reaction device (2) is connected with the pulse type aeration system (3) through a pipeline, and one side of the multi-stage series draft tube reaction device (2) is connected with the membrane interception water outlet system (4) through a pipeline;
the three-point water inlet system (1) comprises a water inlet tank (1-1), the top of the water inlet tank (1-1) is connected with a nutritive salt adding device, one end of the top of the water inlet tank (1-1) is provided with a stock solution inlet (1-2), the stock solution inlet is provided with a stock solution inlet control valve (1-3), one side of the water inlet tank (1-1) is provided with a water outlet a (1-4), and the stock solution inlet (1-2) and the water outlet a (1-4) are respectively positioned at two opposite sides of the water inlet tank (1-1); the nutrient salt feeding device comprises a plurality of sequentially connected bins (1-5), each bin (1-5) is connected to the top of a water inlet tank (1-1) through a batcher (1-6), the nutrient salt feeding device also comprises a stirring motor (1-7) installed at the top of the water inlet tank (1-1), one end of the stirring motor (1-7) is connected with a stirrer (1-8), and the stirrer (1-8) extends into the water inlet tank (1-1); the water outlet a (1-4) is connected with the multistage series draft tube reaction device (2) through a pipeline, and a water inlet pump (1-9), an electromagnetic valve (1-10) and a flowmeter a (1-11) are sequentially arranged on the connecting pipeline;
the PLC automatic control system (5) comprises a PLC automatic control box (5-1) and a computer (5-2), and the computer (5-2) is connected with the PLC automatic control box (5-1); a liquid level control sensor (5-3) connected with a PLC automatic control box (5-1) is arranged in the water inlet tank (1-1), and the tops of the plurality of bins (1-5) are connected to the PLC automatic control box (5-1) through lines;
the working method of the three-point water inlet system (1) comprises the following steps: opening a stock solution inlet control valve (1-3), enabling raw water to enter a water inlet tank (1-1) from a stock solution inlet (1-2), uploading detection data to a PLC automatic control box (5-1) by a liquid level control sensor (5-3), transmitting the data to a computer (5-2) by the PLC automatic control box (5-1) for integrated calculation, then the feed bin (1-5) is controlled to feed nutritive salt into the water inlet tank (1-1) through the batcher (1-6), the stirring motor (1-7) drives the stirrer (1-8) to stir raw water in the water inlet tank, the raw water flows out from the water outlet a (1-4) after being treated, the mixture enters a multi-stage series draft tube reaction device (2) after passing through a water inlet pump (1-9), an electromagnetic valve (1-10) and a flowmeter a (1-11);
the multistage series draft tube reaction device (2) comprises an outer tube (2-1), three two-pole conical inner tubes (2-2) which are connected in sequence are arranged in the outer tube (2-1), namely a first-stage draft tube inner tube (2-2-1), a second-stage draft tube inner tube (2-2-2) and a third-stage draft tube inner tube (2-2-3), and the first-stage draft tube inner tube (2-2-1), the second-stage draft tube inner tube (2-2-2) and the third-stage draft tube inner tube (2-2-3) are different in height and are sequentially arranged from high to low; the conicity of the two-pole conical inner cylinder (2-2) is 1: 0.35 at the height of the two-pole conical inner cylinder (2-2)
Segmenting, wherein the segmentation distance is 40 mm; gas distributors (2-5) are arranged below the three two-pole conical inner cylinders (2-2), and the three gas distributors (2-5) respectively convey gas to the inner parts of the first-stage guide cylinder inner cylinder (2-2-1), the second-stage guide cylinder inner cylinder (2-2-2) and the third-stage guide cylinder (2-2-3); the outer cylinder (2-1), one side of the outer cylinder (2-1) is provided with a water inlet a (2-3), the other side of the outer cylinder (2-1) is provided with a water outlet b (2-4), the top of the outer cylinder (2-1) is provided with a water inlet b (2-6), a water inlet c (2-7) and an air outlet (2-8), the air outlet (2-8) is positioned between the water inlet b (2-6) and the water inlet c (2-7), the bottom of the outer cylinder (2-1) is provided with an air inlet a (2-9), an air inlet b (2-10) and an air inlet c (2-11), the air inlet a (2-9) is positioned below the first-level guide cylinder inner cylinder (2-2-1), the air inlet b (2-10) is positioned below the second-level guide cylinder inner cylinder (2-2-2), and the air inlet c (2-11) is positioned below the third-level guide cylinder (2-2-3); the water inlet a (2-3) is connected with a water outlet a (1-4) of the three-point water inlet system (1) through a pipeline, and the water outlet b (2-4) is connected with a membrane interception water outlet system (4) through a pipeline; the air inlets a (2-9), the air inlets b (2-10) and the air inlets c (2-11) are connected to the pulse type aeration system (3) through pipelines; sensor groups (5-4) are arranged in the three two-pole conical inner cylinders (2-2);
pretreated raw water is respectively treated by a water inlet a (2-3), a water inlet b (2-6), a water inlet c (2-7) and a water inlet ratio of 7: 2: 1, gas enters an outer cylinder (2-1), the gas enters a bipolar conical inner cylinder (2-2) from a gas distributor (2-5) at the bottom, the gas phase content of the bipolar conical inner cylinder (2-2) is larger than that of the outer cylinder (2-1), density difference is formed between fluid inside and outside a guide cylinder reaction device, the density difference forms the driving force of integral circular flow in the guide cylinder reaction device under the action of gravity, mixed fluid with small density in the bipolar conical inner cylinder (2-2) flows upwards, mixed fluid with large density in an outer ring space flows downwards, and then gas-liquid two-phase flow continuously flows upwards into the outer cylinder (2-1) from the bipolar conical inner cylinder (2-2) and then flows downwards into the bipolar conical inner cylinder (2-2) from the outer cylinder (2-1) for circular flow; in the circulating flow process, gas-liquid mixed fluid on the upper part of the first-stage guide cylinder inner cylinder (2-2-1) overflows and flows to the second-stage guide cylinder inner cylinder (2-2-2), gas in the second-stage guide cylinder inner cylinder (2-2-2) enters from the bottom gas distributor (2-5), gas-liquid two-phase flows in the same-stage guide cylinder inner cylinder, gas-liquid mixed fluid on the upper part overflows and flows to the third-stage guide cylinder (2-2-3), gas in the third-stage guide cylinder (2-2-3) enters from the bottom gas distributor (2-5), gas-liquid two-phase flows in the same-stage guide cylinder inner cylinder, and finally flows out from the right-side water outlet b (2-4).
2. A draft tube loop reactor according to claim 1, wherein the pulse type aeration system (3) comprises a plurality of pulse generating devices connected in sequence, one side of the pulse generating device is connected with an air compressor (3-1), the number of the pulse generating devices is the same as the number of the air inlets of the multi-stage series draft tube reaction device (2), and the pulse generating devices are connected with the air inlets of the multi-stage series draft tube reaction device (2) in a one-to-one correspondence manner.
3. The draft tube loop reactor according to claim 1, wherein the membrane interception water outlet system (4) comprises a hollow fiber membrane module (4-1), the bottom end of the hollow fiber membrane module (4-1) is connected with the water outlet b (2-4) of the multi-stage series draft tube reaction device (2) through a pipeline, a raw water pump (4-2) and a safety filter (4-3) are arranged on a connecting pipeline between the bottom end of the hollow fiber membrane module (4-1) and the water outlet b (2-4), and an air compressor (4-5) is connected through an air inlet valve (4-4); the top end of the hollow fiber membrane component (4-1) is connected with the backwashing water tank (4-6) through a pipeline.
4. A draft tube loop reactor according to claim 1, wherein said PLC automatic control system (5) further comprises sensors including level control sensors (5-3) respectively disposed in the water inlet tank (1-1) and the backwash water tank (4-6), further comprising sensor groups (5-4) respectively disposed in each inner tube (2-2), said sensor groups (5-4) comprising a temperature sensor, a DO sensor, a pH sensor and an ORP sensor.
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