CN110357366B - Biochemical treatment method for Fischer-Tropsch synthesis wastewater - Google Patents
Biochemical treatment method for Fischer-Tropsch synthesis wastewater Download PDFInfo
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Abstract
The invention relates to a biochemical treatment process for Fischer-Tropsch synthesis reaction wastewater, and aims to provide a biochemical process capable of directly treating acidic Fischer-Tropsch synthesis wastewater, which can effectively reduce the COD value in the wastewater without adding alkali for neutralization. The treatment process flow is as follows: (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) and precipitating the effluent of the aerobic tank. The process avoids adding alkali for neutralization, greatly reduces the treatment cost, and improves the stability of the flora through the strain selector.
Description
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. A Fischer-Tropsch synthesis wastewater biochemical treatment method comprises the following treatment process flows of (1) discharging Fischer-Tropsch synthesis wastewater into a buffer pool; (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 method is characterized in that:
a container is arranged between a buffer pool and an anaerobic reactor of the Fischer-Tropsch synthesis wastewater biochemical treatment device and is used as a strain selector; 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 specific operating parameter conditions were 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 volume of the strain selector is 1/10-1/4 of that of the anaerobic reactor; the strain selector simultaneously receives the backflow of the effluent mixed liquid of the aerobic tank, wherein the backflow amount accounts for 1/20-1/8 of the water inflow of the aerobic tank; separating acid-resistant flora, and continuously feeding the acid-resistant flora and the Fischer-Tropsch synthesis wastewater obtained by separation into an anaerobic reactor;
3) 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 = 2-8 days, temperature is 32-40 ℃, and total suspended solid content TSS is controlled to be 5-10 kg/m through inflow and retention time3；
4) 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 = 10-20 h and the temperature to be 15-30 ℃, and the total suspended solid is controlled by the inflow and the retention timeThe TSS content is 1-5 kg/m3；
5) Precipitating the mixed liquid of the rest effluent of the aerobic tank to obtain residual sludge and a treated water body;
the structure of the strain selector is a closed cylindrical tank body, an inclined plate separator or an inclined plate sedimentation separator is arranged at the upper part in the tank body, a water distributor is arranged at the middle part in the tank body, and the operation mode of the strain selector is an up-flow mode; the upper part of the tank body is cylindrical, and the lower part of the tank body is hollow and inverted cone-shaped or inverted cone frustum-shaped; the effluent and the return sludge of the buffer tank enter 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 at the upper part are formed by sludge particles and water in the sludge mixed liquor, part of sludge sinks into the bottom, and the other part of sludge is discharged and enters a subsequent anaerobic reactor; an overflow device or an overflow groove is arranged at the center of the top of the reactor and 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.
2. The method of claim 1, wherein: the anaerobic reactor is inoculated with anaerobic Expanded Granular Sludge Bed (EGSB) granular sludge, the inoculation sludge amount is 5-15% of the water inflow, the aerobic tank is inoculated with ordinary urban domestic sludge, the inoculation sludge amount is 20-30% of the volume of the aerobic tank, and extra nutrients do not need to be added.
3. The method of claim 1, wherein: 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.
4. The method of claim 1, wherein: forming a special flora through a strain selector, wherein the designed COD volume load value is 0.20-0.80 kg/m3·d。
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