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CN110357366B - Biochemical treatment method for Fischer-Tropsch synthesis wastewater - Google Patents

Biochemical treatment method for Fischer-Tropsch synthesis wastewater Download PDF

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CN110357366B
CN110357366B CN201910745027.6A CN201910745027A CN110357366B CN 110357366 B CN110357366 B CN 110357366B CN 201910745027 A CN201910745027 A CN 201910745027A CN 110357366 B CN110357366 B CN 110357366B
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anaerobic reactor
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tank
wastewater
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张永军
徐炎华
陆曦
孙文全
于杨
何益得
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Nanjing Tech University
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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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • 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
    • C02F2001/007—Processes including a sedimentation step
    • 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
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • 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
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Abstract

本发明涉及一种费托合成反应废水生化处理工艺，本发明的目的是提供能够直接处理酸性费托合成废水的生化工艺，无须加碱中和操作，即可有效降低废水中COD值。其处理工艺流程为：(1)将费托合成废水排进缓冲池；(2)缓冲池出水进入菌种选择器，该设备同时接收兼氧池混合液回流；(3)菌种选择器出水进入厌氧反应器；(3)采用厌氧反应器出水进行处理；(4)好氧池部分混合液回流至菌种选择器；(5)对好氧池出水进行沉淀。该工艺具有避免了加碱中和，大幅降低了处理成本，并通过菌种选择器，提升了菌群的稳定性。

Figure 201910745027

The invention relates to a biochemical treatment process for Fischer-Tropsch synthesis reaction wastewater, and the purpose of the invention is to provide a biochemical process that can directly treat acidic Fischer-Tropsch synthesis wastewater, and can effectively reduce the COD value in wastewater without adding alkali for neutralization. The treatment process is as follows: (1) discharge the Fischer-Tropsch synthesis wastewater into the buffer pool; (2) the effluent from the buffer pool enters the bacterial species selector, and the device simultaneously receives the backflow of the mixed solution of the facultative oxygen pool; (3) the effluent from the bacterial species selector Enter the anaerobic reactor; (3) use the effluent of the anaerobic reactor for treatment; (4) return part of the mixed liquid of the aerobic tank to the bacterial strain selector; (5) carry out sedimentation of the effluent of the aerobic tank. The process has the advantages of avoiding alkali neutralization, greatly reducing the processing cost, and improving the stability of the bacterial flora through the bacterial species selector.

Figure 201910745027

Description

Biochemical treatment method for Fischer-Tropsch synthesis wastewater
Technical Field
The invention belongs to the field of industrial sewage treatment, and particularly relates to a Fischer-Tropsch synthesis wastewater biochemical treatment process which is suitable for industrial wastewater with high concentration and strong acidity generated in the Fischer-Tropsch synthesis process of coal chemical industry.
Technical Field
Coal chemical industry is an important industry in China, and coal is used as a raw material and is converted into gas, liquid and solid products. Fischer-Tropsch synthesis (Fischer-Tropsch synthesis) is one of the important technical routes for coal indirect liquefaction, and liquid mixed hydrocarbons and oxygen-containing compounds are synthesized by taking synthesis gas (mixed gas of carbon monoxide and hydrogen) as a raw material under a catalyst and proper conditions. The process can produce a great deal of waste water with high concentration and strong acidity, the Chemical Oxygen Demand (COD) concentration is about 15000-35000 mg/L, and the pH range is about 2-4. The general treatment process of the wastewater usually needs to be adjusted to be near neutral pH by adding alkali (Wujinwei, etc., industrial water treatment, 2015, 11: 56-59; Tianzhong, etc., water treatment technology, 2017, 9: 101-. When the waste water needs to be reused, a membrane treatment (ultrafiltration and reverse osmosis) unit is generally added, and the effluent of the biochemical treatment unit is recovered. The waste water treatment process is not provided with a strain selector, so that flora suitable for Fischer-Tropsch waste water treatment cannot be formed, and the treatment process has the following prominent defects: 1) the alkali consumption is large, the cost is high, and a large amount of alkali is required to be added to adjust the pH to be neutral due to lower pH; 2) the energy consumption of the reverse osmosis process is high, the salt content of the wastewater is improved by adding the alkali, the osmotic pressure is increased, and the energy consumption of the reverse osmosis process is improved; 3) the recovery rate of purified water is low, the yield of strong brine is high, and the energy consumption of the evaporator is increased; 4) the waste salt slag has large yield and high solid waste disposal cost. The source of the problems lies in the neutralization by adding alkali, the invention adopts a novel biochemical process and equipment, screens out the specific flora suitable for the treatment of the Fischer-Tropsch wastewater by arranging a strain selector, can treat the Fischer-Tropsch synthetic wastewater without adding alkali, and has neutral pH value of effluent and COD value less than 100 mg/L.
The invention designs a special flora selector on the basis of the original Fischer-Tropsch synthesis wastewater treatment process, performs environmental screening through acidic wastewater, performs mechanical screening by combining hydraulic conditions and a reactor structure, finally forms acid-resistant anaerobic flora, and performs flora supplement on an anaerobic reactor. The flora selector is a closed cylindrical tank, the upper part of the tank is provided with an inclined plate separator (or an inclined plate sedimentation separator), the middle part of the tank is provided with a water distributor, and the operation mode is an up-flow mode. As shown in FIG. 2, the upper part of the reactor is cylindrical, and the lower part is inverted conical (or inverted truncated cone-shaped). The return sludge enters the reactor through a water distributor in the reactor through a water inlet pipe on the side surface of the middle part, a centrifugal force difference formed along the reactor and an inclined plate separator on the upper part are formed by sludge particles and water in the sludge mixed liquor, and part of sludge is sunk into the bottom and discharged to enter a subsequent anaerobic tank. An overflow device (with the depth of 0.5 meter) (or an overflow groove) is arranged at the central position of the top of the reactor (above the inclined plate separator), and the edge of a liquid inflow end at the upper end of the overflow device is serrated. The wastewater enters a drain pipe through an overflow device and is discharged out of the reactor. The specific design parameters are marked in the figure, and other requirements are as follows: H/D is 1.5-2.0, and D/D is 0.5. After the acid wastewater and the mixed liquid in the aerobic tank flow back, the acid wastewater enters the flora selector from the water distributor at the bottom and releases anaerobic bacteria in the zoogloea under the action of hydraulic shearing. The mud-water mixture flows through a solid-liquid separator at the upper part, and large-particle sludge is separated and sinks. The flora passing through the solid-liquid separator flows out of the flora selector from the upper part to be used as a supplementary strain and enters an anaerobic reaction system.
The technical problem to be solved by the discovery is how to directly treat the Fischer-Tropsch synthesis wastewater by adopting an anaerobic method, so that the system problem caused by adding alkali for neutralization is avoided, and finally, the purpose of greatly reducing the comprehensive cost of treating and recycling the Fischer-Tropsch synthesis wastewater is realized.
Disclosure of Invention
The invention relates to a biochemical treatment process for Fischer-Tropsch synthesis wastewater, and aims to provide a biochemical treatment process for Fischer-Tropsch synthesis wastewater with a low pH value, which can effectively reduce the COD value in the wastewater.
1. A biochemical treatment process for Fischer-Tropsch synthesis wastewater comprises the following treatment process flows:
(1) discharging the Fischer-Tropsch synthesis wastewater into a buffer tank; (2) the effluent of the buffer tank enters a strain selector, and the device simultaneously receives the mixed liquid reflux of the facultative tank; (3) the effluent of the strain selector enters an anaerobic reactor; (3) treating the effluent of the anaerobic reactor; (4) part of mixed liquid in the aerobic tank flows back to the strain selector; (5) precipitating the effluent of the aerobic tank to obtain excess sludge, wherein the specific parameter conditions are as follows:
(1) sending the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 5,000-25,000 mg/L, the pH is 2.5-4.0, and the temperature is 15-40 ℃;
(2) arranging a strain selector between the buffer pool and the anaerobic reactor, wherein the effective volume of the strain selector is 1/10-1/4 of the anaerobic reactor; the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculated sludge amount is 5-15% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculated sludge amount is 20-30% of the tank volume, and no extra nutrient is added.
(3) The strain selector simultaneously receives the backflow of the mixed liquid in the aerobic tank, wherein the backflow amount accounts for 1/20-1/8 of the water inflow amount of the aerobic tank; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater continuously enter an anaerobic reactor;
(4) the strain selector simultaneously receives the effluent of the buffer tank and separates acid-resistant flora; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater enter an anaerobic reactor together;
(5) the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the conditions of the anaerobic reactor are that hydraulic retention time HRT is 2-8 days, the temperature is 32-40 ℃, and the total suspended solid content TSS is controlled to be 5-10 kg/m by water inflow and retention time3；
(6) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, meanwhile, part of mixed liquor in the aerobic tank flows back to a strain selector, the aerobic tank leads the dissolved oxygen in the tank to be 2.0-4.0 mg/L through aeration, the hydraulic retention time HRT is 10-20 h, the temperature is 15-30 ℃, and the total suspended solid content TSS is controlled to be 1-5 kg/m through the inflow and the retention time3；
The pH value of the wastewater in the buffer pool is kept between 2.5 and 4.0.
A strain selector is arranged in front of the anaerobic reactor, and the effective volume of the strain selector is 1/10-1/5 of the anaerobic reactor.
The strain selector receives the backflow of the mixed liquid in the aerobic tank, and the backflow amount accounts for 1/20-1/8 of the water inflow.
The A/O system forms a special flora through a strain selector, and the design value of COD (chemical oxygen demand) volume load is 0.20-0.80 kg/m3·d。
The invention has the following outstanding characteristics: 1) the pH value of the wastewater is not required to be adjusted by adding alkali; 2) separating and enriching acid-resistant flora from the denitrification sludge by adopting a flora selector without continuously adding strains; 3) the high-acid wastewater firstly enters a flora selector and then enters an anaerobic system.
Drawings
FIG. 1 shows a process for biochemical treatment of Fischer-Tropsch synthesis wastewater;
FIG. 2 is a schematic diagram of a strain selector. FIG. 1 shows an overflow device; 2. a drain pipe; 3. a water inlet pipe; 4. an inclined plate separator, 5, a mud pipe.
Detailed Description
Comparative example 1:
a Fischer-Tropsch synthesis wastewater biochemical treatment process comprises (1) discharging Fischer-Tropsch synthesis wastewater into a buffer tank; (2) the effluent of the buffer tank enters an anaerobic reactor, and the effluent of the buffer tank is treated by the anaerobic reactor; (3) the effluent of the anaerobic reactor enters an aerobic tank, and the effluent of the anaerobic reactor is treated by the aerobic tank; (4) precipitating the mixed liquid of the effluent of the aerobic tank to obtain excess sludge and a treated water body;
the original treatment process flow comprises the following steps:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 21,000mg/L, the pH value is 3.5, the temperature is 20 ℃, and calcium oxide is added into the buffer tank to ensure that the pH value of the effluent is 7;
(2) the effluent of the buffer tank enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the conditions of the anaerobic reactor are that hydraulic retention time HRT is 2-8 days, the temperature is 35 ℃, and the total suspended solid content TSS is controlled to be 8kg/m through inflow and retention time3；
(3) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, the aerobic tank leads dissolved oxygen in the tank to be 3.0mg/L through aeration, the hydraulic retention time HRT is 15h, the temperature is 20 ℃, and the total suspended solid content TSS is controlled to be 3kg/m through the inflow and the retention time3；
(4) After the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 598mg/L, the pH is 7, and the TSS is 30 mg/L.
Example 1
Arranging a container as a strain selector between a buffer pool and an anaerobic reactor of the Fischer-Tropsch synthesis wastewater biochemical treatment device in the operating comparative example 1; the effluent of the buffer tank enters a strain selector, and the strain selector simultaneously receives partial reflux water of the effluent mixed liquor of the aerobic tank; the effluent of the strain selector enters an anaerobic reactor; part of effluent mixed liquor of the aerobic tank flows back to the strain selector;
a biochemical treatment process for Fischer-Tropsch synthesis wastewater comprises the following treatment process flows:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 21,000mg/L, the pH value is 3.5, and the temperature is 20 ℃;
(2) a strain selector is arranged between the buffer pool and the anaerobic reactor, and the effective volume of the strain selector is 1/8 of the anaerobic reactor; the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculated sludge amount is 10% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculated sludge amount is 20% of the tank volume, and no extra nutrient is added.
(3) The strain selector simultaneously receives the mixed liquid reflux of the aerobic tank, and the reflux amount accounts for 1/12 of the water inflow of the aerobic tank; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater continuously enter an anaerobic reactor;
(4) the strain selector simultaneously receives the effluent of the buffer tank and separates acid-resistant flora; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater enter an anaerobic reactor together;
(5) the effluent of the strain selector enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the conditions of the anaerobic reactor are that hydraulic retention time HRT is 2-8 days, the temperature is 35 ℃, and the total suspended solid content TSS is controlled to be 8kg/m through inflow and retention time3；
(6) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, meanwhile, part of mixed liquor in the tank A (the aerobic tank) flows back to a strain selector, the aerobic tank leads dissolved oxygen in the tank to be 3.0mg/L through aeration, the hydraulic retention time HRT is 15h, the temperature is 20 ℃, and the total suspended solid content TSS is controlled to be 3kg/m through the inflow and the retention time3；
(7) After the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 85mg/L, the pH is 6, and the TSS is 20 mg/L. Comparative example 2:
a Fischer-Tropsch synthesis wastewater biochemical treatment process comprises (1) discharging Fischer-Tropsch synthesis wastewater into a buffer tank; (2) the effluent of the buffer tank enters an anaerobic reactor, and the effluent of the buffer tank is treated by the anaerobic reactor; (3) the effluent of the anaerobic reactor enters an aerobic tank, and the effluent of the anaerobic reactor is treated by the aerobic tank; (4) precipitating the mixed liquid of the effluent of the aerobic tank to obtain excess sludge and a treated water body;
the original treatment process flow comprises the following steps:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 21,000mg/L, the pH value is 3.5, the temperature is 20 ℃, and calcium oxide is added into the buffer tank to ensure that the pH value of the effluent is 7;
(2) the effluent of the buffer pool enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the anaerobic reactor is provided with hydraulic retention time HRT (Rockwell temperature) of 5 days and temperature of 30 ℃, and the total suspended solid content TSS is controlled to be 6kg/m by the inflow and retention time3；
(3) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, the aerobic tank leads the dissolved oxygen in the tank to be 2.5mg/L through aeration, the hydraulic retention time HRT is 18h, the temperature is 25 ℃, and the total suspended solid content TSS is controlled to be 2kg/m through the inflow and the retention time3；
(4) After the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 714mg/L, the pH is 7, and the TSS is 53 mg/L.
Example 2:
arranging a container as a strain selector between a buffer pool and an anaerobic reactor of the Fischer-Tropsch synthesis wastewater biochemical treatment device in the operating comparative example 2; the effluent of the buffer tank enters a strain selector, and the strain selector simultaneously receives partial reflux water of the effluent mixed liquor of the aerobic tank; the effluent of the strain selector enters an anaerobic reactor; part of effluent mixed liquor of the aerobic tank flows back to the strain selector;
the treatment process flow is as follows:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 21,000mg/L, the pH value is 3.5, and the temperature is 20 ℃;
(2) a strain selector is arranged between the buffer pool and the anaerobic reactor, and the effective volume of the strain selector is 1/10 of the anaerobic reactor; the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculated sludge amount is 15% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculated sludge amount is 25% of the tank volume, and no extra nutrient is added.
(3) The strain selector simultaneously receives the mixed liquid reflux of the aerobic tank, and the reflux amount accounts for 1/12 of the water inflow of the aerobic tank; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater continuously enter an anaerobic reactor;
(4) the strain selector simultaneously receives the effluent of the buffer tank and separates acid-resistant flora; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater enter an anaerobic reactor together;
(5) the effluent of the strain selector enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the anaerobic reactor is provided with hydraulic retention time HRT (Rockwell temperature) of 5 days and temperature of 30 ℃, and the total suspended solid content TSS is controlled to be 6kg/m by the inflow and retention time3；
(6) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, meanwhile, part of mixed liquor in the tank A flows back to a strain selector, the aerobic tank leads the dissolved oxygen in the tank to be 2.5mg/L through aeration, the hydraulic retention time HRT is 18h, the temperature is 25 ℃, and the total suspended solid content TSS is controlled to be 2kg/m through the inflow and the retention time3；
(7) After the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 75mg/L, the pH is 6.5, and the TSS is 18 mg/L. Comparative example 3:
a Fischer-Tropsch synthesis wastewater biochemical treatment process comprises (1) discharging Fischer-Tropsch synthesis wastewater into a buffer tank; (2) the effluent of the buffer tank enters an anaerobic reactor, and the effluent of the buffer tank is treated by the anaerobic reactor; (3) the effluent of the anaerobic reactor enters an aerobic tank, and the effluent of the anaerobic reactor is treated by the aerobic tank; (4) precipitating the mixed liquid of the effluent of the aerobic tank to obtain excess sludge and a treated water body;
the original treatment process flow comprises the following steps:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 25,000mg/L, the pH is 3.2, the temperature is 30 ℃, and calcium oxide is added into the buffer tank to ensure that the pH of the effluent is 7;
(2) the effluent of the buffer pool enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the conditions of the anaerobic reactor are that hydraulic retention time HRT is 6 days, the temperature is 32 ℃, and the total suspended solid content TSS is controlled to be 7kg/m by water inflow and retention time3；
(3) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, the aerobic tank leads dissolved oxygen in the tank to be 3.2mg/L through aeration, the hydraulic retention time HRT is 18h, the temperature is 27 ℃, and the total suspended solid content TSS is controlled to be 4kg/m through the inflow and the retention time3；
(4) After the stable operation is carried out for 72 hours, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 625mg/L, the pH is 7, and the TSS is 56 mg/L.
Example 3:
arranging a container as a strain selector between a buffer pool and an anaerobic reactor of the Fischer-Tropsch synthesis wastewater biochemical treatment device in the operating comparative example 3; the effluent of the buffer tank enters a strain selector, and the strain selector simultaneously receives partial reflux water of the effluent mixed liquor of the aerobic tank; the effluent of the strain selector enters an anaerobic reactor; part of effluent mixed liquor of the aerobic tank flows back to the strain selector;
a biochemical treatment process for Fischer-Tropsch synthesis wastewater comprises the following treatment process flows:
(1) sending the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 25,000mg/L, the pH value is 3.2, and the temperature is 30 ℃;
(2) a strain selector is arranged between the buffer pool and the anaerobic reactor, and the effective volume of the strain selector is 1/8 of the anaerobic reactor; the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculated sludge amount is 15% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculated sludge amount is 25% of the tank volume, and no extra nutrient is added.
(3) The strain selector simultaneously receives the mixed liquid reflux of the aerobic tank, and the reflux amount accounts for 1/15 of the water inflow of the aerobic tank; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater continuously enter an anaerobic reactor;
(4) the strain selector simultaneously receives the effluent of the buffer tank and separates acid-resistant flora; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater enter an anaerobic reactor together;
(5) the effluent of the strain selector enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the anaerobic reactor is provided with hydraulic retention time HRT (Rockwell hardness) of 6 days and temperature of 32 ℃, and the total suspended solid content TSS is controlled to be 7kg/m3 by inflow and retention time;
(6) the effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, meanwhile, part of mixed liquor in the tank A flows back to a strain selector, the aerobic tank leads dissolved oxygen in the tank to be 3.2mg/L through aeration, the hydraulic retention time HRT is 18h, the temperature is 27 ℃, and the total suspended solid content TSS is controlled to be 4kg/m3 through the inflow and the retention time;
(7) after the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 78mg/L, the pH is 6.2, and the TSS is 19 mg/L.
Comparative example 4:
a Fischer-Tropsch synthesis wastewater biochemical treatment process comprises (1) discharging Fischer-Tropsch synthesis wastewater into a buffer tank; (2) the effluent of the buffer tank enters an anaerobic reactor, and the effluent of the buffer tank is treated by the anaerobic reactor; (3) the effluent of the anaerobic reactor enters an aerobic tank, and the effluent of the anaerobic reactor is treated by the aerobic tank; (4) precipitating the mixed liquid of the effluent of the aerobic tank to obtain excess sludge and a treated water body;
the original treatment process flow comprises the following steps:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 10,000mg/L, the pH is 2.8, the temperature is 29 ℃, and calcium oxide is added into the buffer tank to ensure that the pH of the effluent is 7;
(2) the effluent of the buffer pool enters an anaerobic reactor, the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into methane, the anaerobic reactor is provided with hydraulic retention time HRT (Rockwell temperature) of 5 days and temperature of 36 ℃, and the total suspended solid content TSS is controlled to be 9kg/m by the inflow and retention time3；
(3) The effluent of the anaerobic reactor enters an aerobic tank to further degrade organic matters in the wastewater, the aerobic tank leads dissolved oxygen in the tank to be 3.8mg/L through aeration, the hydraulic retention time HRT is 20h, the temperature is 28 ℃, and the total suspended solid content TSS is controlled to be 5kg/m through the inflow and the retention time3；
(4) After the stable operation for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 697mg/L, the pH is 7, and the TSS is 52 mg/L.
Example 4:
arranging a container as a strain selector between a buffer pool and an anaerobic reactor of the Fischer-Tropsch synthesis wastewater biochemical treatment device in the operating comparative example 4; the effluent of the buffer tank enters a strain selector, and the strain selector simultaneously receives partial reflux water of the effluent mixed liquor of the aerobic tank; the effluent of the strain selector enters an anaerobic reactor; part of effluent mixed liquor of the aerobic tank flows back to the strain selector;
a biochemical treatment process for Fischer-Tropsch synthesis wastewater comprises the following treatment process flows:
(1) sending the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 10,000mg/L, the pH value is 2.8, and the temperature is 29 ℃;
(2) a strain selector is arranged between the buffer pool and the anaerobic reactor, and the effective volume of the strain selector is 1/8 of the anaerobic reactor; the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculated sludge amount is 20% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculated sludge amount is 20% of the tank volume, and no extra nutrient is added.
(3) The strain selector simultaneously receives the mixed liquid reflux of the aerobic tank, and the reflux amount accounts for 1/9 of the water inflow of the aerobic tank; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater continuously enter an anaerobic reactor;
the strain selector simultaneously receives the effluent of the buffer tank and separates acid-resistant flora; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater enter an anaerobic reactor together;
(4) the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor, converts the organic substances into biogas, and is provided with hydraulic retention time HRT of 5 days and temperature of 36 ℃, and the total suspended solid content TSS is controlled to be 9kg/m by water inflow and retention time3；
(5) The effluent of the strain selector enters an anaerobic reactor, the effluent of the anaerobic reactor enters an aerobic tank, organic matters in the wastewater are further degraded, meanwhile, part of mixed liquor in the tank A flows back to the strain selector, the aerobic tank leads the dissolved oxygen in the tank to be 3.8mg/L through aeration, the hydraulic retention time HRT is 20h, the temperature is 28 ℃, and the total suspended solid content TSS is controlled to be 5kg/m through the inflow and the retention time3；
(6) After the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 74mg/L, the pH is 6.1, and the TSS is 16 mg/L.
Example 5:
a biochemical treatment process for Fischer-Tropsch synthesis wastewater comprises the following treatment process flows:
(1) feeding the Fischer-Tropsch synthesis wastewater into a buffer tank, wherein the COD (chemical oxygen demand) of the wastewater collected by the buffer tank is 21,000mg/L, the pH value is 3.5, and the temperature is 20 ℃;
(2) a strain selector is arranged between the buffer pool and the anaerobic reactor, and the effective volume of the strain selector is 1/8 of the anaerobic reactor; the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculated sludge amount is 10% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculated sludge amount is 20% of the tank volume, and no extra nutrient is added.
(3) The strain selector simultaneously receives the mixed liquid reflux of the aerobic tank, and the reflux amount accounts for 1/12 of the water inflow of the aerobic tank; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater continuously enter an anaerobic reactor;
the strain selector simultaneously receives the effluent of the buffer tank and separates acid-resistant flora; the acid-resistant bacteria obtained by separation and the Fischer-Tropsch synthesis wastewater enter an anaerobic reactor together;
(4) the anaerobic reactor degrades organic substances in the wastewater by using acid-resistant flora and other flora in the anaerobic reactor and converts the organic substances into biogas, the conditions of the anaerobic reactor are that hydraulic retention time HRT is 2-8 days, the temperature is 35 ℃, and the total suspended solid content TSS is controlled to be 8kg/m by inflow and retention time3；
(5) The effluent of the strain selector enters an anaerobic reactor, the effluent of the anaerobic reactor enters an aerobic tank, organic matters in the wastewater are further degraded, meanwhile, part of mixed liquor in the tank A flows back to the strain selector, the aerobic tank leads the dissolved oxygen in the tank to be 3.0mg/L through aeration, the hydraulic retention time HRT is 15h, the temperature is 20 ℃, and the total suspended solid content TSS is controlled to be 3kg/m through the inflow and the retention time3；
(6) After the stable operation is carried out for 72h, the effluent of the aerobic tank realizes mud-water separation, one part of sludge flows back to the strain selector, the other part of sludge is discharged out of the aerobic tank, the COD of the effluent of the aerobic tank is 85mg/L, the pH is 6, and the TSS is 20 mg/L.

Claims (4)

1.一种费托合成废水生化处理方法，其处理工艺流程为，（1）将费托合成废水排进缓冲池；（2）缓冲池出水进入厌氧反应器，采用厌氧反应器对缓冲池出水进行处理；（3）厌氧反应器出水进入好氧池，采用好氧池对厌氧反应器出水进行处理；（4）对好氧池出水混合液进行沉淀，获得剩余污泥和处理后的水体；其特征在于：1. A method for biochemical treatment of Fischer-Tropsch synthesis wastewater, the process of which is as follows: (1) discharge Fischer-Tropsch synthesis wastewater into a buffer tank; (2) effluent from the buffer tank enters an anaerobic reactor, and the anaerobic reactor is used to buffer the (3) The effluent of the anaerobic reactor enters the aerobic tank, and the effluent of the anaerobic reactor is treated by the aerobic tank; (4) The mixed liquid of the effluent from the aerobic tank is precipitated to obtain excess sludge and treated body of water after; characterized by: 于费托合成废水生化处理装置的缓冲池和厌氧反应器之间设置一容器作为菌种选择器；缓冲池出水进入菌种选择器，菌种选择器同时接收好氧池出水混合液的部分回流水；菌种选择器出水进入厌氧反应器；好氧池部分出水混合液回流至菌种选择器；具体运行参数条件如下：A container is set between the buffer tank and the anaerobic reactor of the Fischer-Tropsch synthesis wastewater biochemical treatment device as a strain selector; the effluent from the buffer tank enters the strain selector, and the strain selector simultaneously receives part of the mixed solution of the effluent from the aerobic tank Return water; the effluent from the strain selector enters the anaerobic reactor; part of the effluent mixture from the aerobic tank returns to the strain selector; the specific operating parameters are as follows: 1）将费托合成废水送入缓冲池，缓冲池收集废水的COD处于5,000~25,000mg/L，pH为2.5~4.0，温度为15~40 ℃；1) Send the Fischer-Tropsch synthesis wastewater into the buffer tank, the COD of the wastewater collected in the buffer tank is 5,000~25,000mg/L, the pH is 2.5~4.0, and the temperature is 15~40 ℃; 2）在缓冲池和厌氧反应器间，设置菌种选择器，其体积为厌氧反应器的1/10~1/4；该菌种选择器同时接收好氧池的出水混合液回流，回流量占好氧池进水量的1/20~1/8；对耐酸菌群进行分离，分离得到的耐酸菌和费托合成废水一起连续进入厌氧反应器；2) Between the buffer tank and the anaerobic reactor, a strain selector is set up, and its volume is 1/10~1/4 of the anaerobic reactor; the strain selector also receives the effluent mixture from the aerobic tank and returns, The return flow accounts for 1/20~1/8 of the water inflow of the aerobic tank; the acid-resistant bacteria group is separated, and the separated acid-resistant bacteria and the Fischer-Tropsch synthesis wastewater continuously enter the anaerobic reactor; 3）厌氧反应器利用厌氧反应器中的耐酸菌群和其它菌群降解废水中的有机物质，将其转化为沼气，厌氧反应器条件为水力停留时间HRT=2~8天，温度为32℃~40℃，通过进水流量及停留时间控制总悬浮固体含量TSS为5~10 kg/m3；3) The anaerobic reactor uses the acid-resistant bacteria and other bacteria in the anaerobic reactor to degrade the organic matter in the wastewater and convert it into biogas. The conditions of the anaerobic reactor are hydraulic retention time HRT=2~8 days, temperature The temperature is 32℃~40℃, and the total suspended solid content TSS is controlled to be 5~10 kg/m 3 by the influent flow rate and residence time; 4）厌氧反应器出水进入好氧池，进一步降解废水中的有机物，同时好氧池中的部分混合液回流到菌种选择器，好氧池通过曝气使池内溶解氧2.0~4.0 mg/L，水力停留时间HRT=10~20 h，温度为15℃~30℃，通过进水流量及停留时间控制总悬浮固体含量TSS为1~5 kg/m3；4) The effluent of the anaerobic reactor enters the aerobic tank to further degrade the organic matter in the wastewater. At the same time, part of the mixed liquid in the aerobic tank is returned to the bacteria selector, and the aerobic tank is aerated to make the dissolved oxygen in the tank 2.0~4.0 mg/ L, the hydraulic retention time HRT=10~20 h, the temperature is 15℃~30℃, and the total suspended solid content TSS is controlled to be 1~5 kg/m 3 by the influent flow rate and residence time; 5）对好氧池其余部分出水混合液进行沉淀，获得剩余污泥和处理后的水体；5) Precipitate the rest of the effluent mixture of the aerobic tank to obtain excess sludge and treated water; 所述菌种选择器的结构为密闭圆柱形罐体，罐体内的上部设有斜板分离器或斜板沉降分离器或斜板沉淀分离器，罐体内的中部设有布水器，菌种选择器的运行方式为上流式；罐体上部为圆筒形，下部为中空的倒圆锥形或倒圆锥台形；缓冲池出水和回流污泥通过中部侧面的进水管经反应器内部的布水器进入反应器，通过污泥混合液中污泥颗粒和水形成沿反应器形成的离心力差异及上部的斜板分离器，部分污泥沉入底部，另一部分排放进入后续的厌氧反应器；反应器顶部的中心位置、斜板分离器的上方设置溢流器或溢流槽，溢流器上端液体流入端的边缘为锯齿状；废水通过溢流器进入排水管，排出反应器。The structure of the strain selector is a closed cylindrical tank, the upper part of the tank is provided with a sloping plate separator or an inclined plate sedimentation separator or an inclined plate sedimentation separator, and a water distributor is arranged in the middle of the tank, and the bacteria The operation mode of the selector is upward flow; the upper part of the tank is cylindrical, and the lower part is a hollow inverted conical or inverted conical truncated shape; the effluent of the buffer tank and the return sludge pass through the water inlet pipe on the side of the middle and pass through the water distributor inside the reactor Entering the reactor, the centrifugal force difference formed along the reactor and the upper inclined plate separator are formed by the sludge particles and water in the sludge mixture, part of the sludge sinks to the bottom, and the other part is discharged into the subsequent anaerobic reactor; the reaction An overflow device or overflow tank is arranged at the center of the top of the device and above the inclined plate separator. The edge of the liquid inflow end of the upper end of the overflow device is serrated; the waste water enters the drain pipe through the overflow device and is discharged from the reactor. 2.根据权利要求1所述的方法，其特征在于：所述厌氧反应器内采用厌氧膨胀颗粒污泥床（EGSB）颗粒污泥接种，接种污泥量为进水量的5~15%，好氧池采用普通城市生活污泥接种，接种污泥量为好氧池体积的20~30%，不用投加额外营养物。2 . The method according to claim 1 , wherein the anaerobic expanded granular sludge bed (EGSB) granular sludge is used for inoculation in the anaerobic reactor, and the amount of inoculated sludge is 5-15% of the water inflow. 3 . , The aerobic tank is inoculated with ordinary urban domestic sludge, and the amount of inoculated sludge is 20~30% of the volume of the aerobic tank, without adding additional nutrients. 3.根据权利要求1所述的方法，其特征在于：厌氧反应器前设置菌种选择器，其有效体积为厌氧反应器的1/10~1/5。3. The method according to claim 1, characterized in that: a strain selector is arranged in front of the anaerobic reactor, and its effective volume is 1/10~1/5 of the anaerobic reactor. 4.根据权利要求1所述的方法，其特征在于：通过菌种选择器形成特殊菌群，COD容积负荷设计值为0.20~0.80kg/m3·d。4 . The method according to claim 1 , wherein a special bacterial group is formed through a bacterial species selector, and the COD volume load design value is 0.20-0.80 kg/m 3 ·d. 5 .
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