CN212450860U - Gasification buck removes hard system - Google Patents
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Abstract
The utility model belongs to coal gas gasification sewage treatment field, concretely relates to gasification buck removes hard system, including subsider, new grey water jar, a plurality of parallel operation's many medium filter, a plurality of parallel operation's nanometer filler adsorber, attached analytic unit, grey water accumulator that communicate in proper order. The utility model discloses simple process, the flow is short, and equipment is few, has solved gasifier grey water system hardness height and the scale deposit that causes, blocks up the problem, and it is lower not throw in addition with new medicament play water quality of water stable system running cost in the system in operation. The sewage discharge amount after the grey water treatment is reduced, the sewage treatment difficulty is reduced, the production and operation cost of the sewage is further reduced, the wastewater is recycled, the supplementary water amount of desalted water is greatly saved, and the raw water consumption is further saved; meanwhile, the content of substances such as salt, COD (chemical oxygen demand), ammonia nitrogen and the like in the grey water system can be reduced, and the hardness of water can be reduced, so that the project is worthy of popularization and application in the grey water treatment system.
Description
Technical Field
The utility model belongs to coal gas gasification sewage treatment field, concretely relates to gasification buck removes hard system.
Background
The process of the grey water process cycle of the aerospace coal gasification device comprises the following steps: the high-pressure black water containing a large amount of coal ash solid particles generated in a gasification furnace and a synthesis gas washing tower is treated by processes of pressure reduction, flash evaporation, sedimentation and the like to obtain water with less impurity content, which is called as grey water. High-pressure black water from a chilling chamber of a gasification furnace and a tower bottom of a washing tower is depressurized by a pressure reducing valve and then is sent to a flash evaporation system to remove most solid particles, a flocculating agent is added into the high-pressure black water through a settling tank for settling to obtain clear grey water, a part of the grey water is discharged to wastewater treatment, and a part of the grey water is recycled to the system as process water. And after being deoxidized, the circulating grey water is pressurized by a high-pressure grey water pump and is sent into a gasification washing system for recycling.
The process design of the water circulation system of the aerospace coal gasification device can reduce the salt concentration of the grey water to a certain extent to slow down the scaling rate, simultaneously cause the reduction of the reuse rate of the grey water, increase the operation cost of enterprises and be not in line with the requirements of energy conservation and emission reduction of modern coal chemical enterprises. In addition, a large amount of discharged sewage brings huge pressure to a downstream water treatment system. Therefore, how to reduce the hardness of the grey water, improve the reuse rate of the grey water, reduce the fresh water consumption and reduce the production and operation cost is a difficult point faced by the coal gasification device.
Hardness is an important index for water quality characterization, and refers to metal ions which are easy to form precipitates in water, mainly calcium ions and magnesium ions. The calcium and magnesium ions are combined with sulfate radicals, carbonate radicals and bicarbonate radicals in the water to form the calcium magnesium salt. Hard water can have varying degrees of impact both in life and in industrial processes. When people take a bath with hard water in life, a layer of soap coagulated particle mucosa is left on the skin, so that bacteria on the skin are difficult to eliminate, and even allergic eczema is caused in severe cases. The appearance of the over-hard water in the household vessel is also the obvious phenomenon that the kettle bottom scales when the boiled water is used for a long time, and the phenomenon that the solar pipeline is blocked is the appearance of the over-hard water quality. Hard water is harmful to industry to a certain extent, and scale formed causes many problems in a hot water system, a water supply device and a boiler heat pipeline system, such as scale deposition, poor heat transfer, low efficiency, pipeline blockage and the like, and leads to system paralysis when water using faults are serious.
The method for removing hardness in the ash water by the existing coal gasification process mainly comprises the following steps: membrane technology, chemical method, electrochemistry, ion exchange technology and nano adsorption technology. Now, the technical comparison is carried out on the methods:
the membrane technology comprises the following steps: the hardness of the membrane can be removed by the membrane method, but the water inlet of the membrane device cannot exceed 45 ℃, a heat exchange system needs to be arranged, and circulating water needs to be configured. The device has many supporting facilities, large required circulating water amount, complex management, difficult automation increase, large system floor area and relatively increased construction cost.
The chemical method comprises the following steps: the hardness is removed by a chemical method, a large amount of chemical agents are required to be added, the salt content of the system is increased, the solid waste residue amount is also increased indirectly, meanwhile, a plurality of auxiliary facilities are provided, the requirement on automation control is high, a dosing device and a detection instrument with high precision need to be matched, the quality of effluent of the system is unstable, and the operation cost is high.
Electrochemistry: the technology including electric flocculation, electrolytic descaling and the like can remove hardness, needs to adjust pH value, adds medicaments such as acid and alkali and the like, is difficult to control water quality, has unstable effluent water quality, increases salinity in water and indirectly increases solid residue, and has large equipment floor area and high operating cost.
Ion exchange technology: the hardness can be removed, but the requirements on the suspended matters, COD (chemical oxygen demand), water temperature and heavy metal ions of inlet water are higher, the technology is difficult to adapt to the treatment of high-hardness wastewater, the grey water needs to be cooled and pretreated by adopting the technology, otherwise, resin pollution, poisoning, damage and the like are directly caused, and meanwhile, a large amount of waste liquid needs to be discharged by the ion exchange technology and needs to be treated.
Because the temperature of the gasification ash water of the space gas is high, the technology can not meet the requirements in the principles of safety, reliability, economy and advancement compared with several technologies (mainly membrane technology, chemical method, electrochemistry, ion exchange technology and nano adsorption technology) of the prior gasification ash water treatment comprehensively.
Disclosure of Invention
An object of the utility model is to provide a gasification buck removes hard system, the replenishment water yield of the system that can significantly reduce of this system to can practice thrift the desalination water replenishment volume, not only guarantee system steady operation, economic benefits is showing moreover.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a gasification grey water hardness removal system comprises a settling tank, a new grey water tank, a plurality of multi-medium filters which operate in parallel, a plurality of nano-filler adsorbers which operate in parallel, an auxiliary analysis unit and a grey water recovery tank which are sequentially communicated;
the settling tank is used for preliminarily separating solid from liquid of the raw ash water;
the new ash tank is used for collecting overflow clear liquid of the settling tank;
the multi-medium filter is used for removing colloids and suspended matters in water and ensuring the water inlet requirement of the adsorption device;
the nano filler adsorber is used for adsorbing calcium and magnesium ions in the ash water at high temperature;
the auxiliary analysis unit comprises an analysis device and an analysis liquid recovery processing device, the analysis device is used for storing analysis liquid, pumping the analysis liquid into the nanofiller adsorber through a pipeline and regenerating and analyzing the adsorbent, and the analysis liquid recovery processing device is used for recovering and processing analysis waste liquid;
and the grey water recovery tank is used for collecting the purified grey water and recycling the grey water to the system for further utilization.
Furthermore, quartz sand is filled in the multi-media filter, and an adsorbent inside the nano-filler adsorber is nano-resin particles.
Furthermore, the multi-media filter comprises a first water inlet pipe and a first water outlet pipe, wherein the first water inlet pipe is communicated with the new ash water tank and is arranged at the upper part of the multi-media filter, the first water outlet pipe is arranged at the lower part of the multi-media filter, the first water inlet pipe is provided with a hardness-removing water pump and is used for pumping the ash water in the new ash water tank into the multi-media filter, the first water inlet pipe is correspondingly provided with a first water inlet valve, and the first water outlet pipe is correspondingly provided with a.
Furthermore, the multi-medium filter is also provided with a backwashing module, the backwashing module comprises a backwashing discharge pipe and a first exhaust pipe which are arranged at the top of the multi-medium filter, and a forward washing discharge pipe and an air inlet pipe which are arranged at the bottom of the multi-medium filter, a backwashing discharge valve is correspondingly arranged on the backwashing discharge pipe, a first exhaust valve is arranged on the first exhaust pipe, a forward washing discharge valve is arranged on the forward washing discharge pipe, and an air inlet valve is arranged on the air inlet pipe.
Furthermore, the nano-filler adsorber comprises a second water inlet pipe communicated with the multi-media filter and arranged at the upper part of the nano-filler adsorber, and a second water outlet pipe arranged at the lower part of the nano-filler adsorber, wherein a second water inlet valve is correspondingly arranged on the second water inlet pipe, and a second water outlet valve is correspondingly arranged on the second water outlet pipe.
Furthermore, the nano-filler adsorber is provided with an analytic module, the analytic module comprises a regenerated analytic liquid inlet pipe arranged at the lower part of the nano-filler adsorber and an analytic waste liquid discharge pipe arranged at the upper part of the nano-filler adsorber, and the regenerated analytic liquid inlet pipe and the analytic waste liquid discharge pipe are correspondingly provided with a regenerated analytic liquid inlet valve and an analytic waste liquid discharge valve respectively; the device is characterized by further comprising a backwashing water inlet pipe and a forward washing blow-off pipe which are arranged at the bottom of the nano filler adsorber, and a backwashing blow-off pipe and a second exhaust pipe which are arranged at the top of the nano filler adsorber, wherein a backwashing water inlet valve is arranged on the backwashing water inlet pipe correspondingly, a forward washing blow-off valve is arranged on the forward washing blow-off pipe, a backwashing blow-off valve is arranged on the backwashing blow-off pipe, and a second exhaust valve is arranged on the second exhaust pipe.
Further, the analytic waste liquid discharge pipe is communicated to an analytic liquid recovery processing device, a membrane separation structure is arranged in the analytic liquid recovery processing device, and the membrane separation structure at least comprises an ultrafiltration membrane, a nano-membrane and a reverse osmosis membrane.
Advantageous effects
1. The utility model adds the ash water recovery system on the basis of the existing space gas slag melting and ash water treatment system, the system can remove calcium and magnesium ions, reduce the content of calcium and magnesium ions, and solve the problems of scaling and blockage caused by overhigh hardness of the ash water system of the gasification furnace; the problem of gradually removing the scale-forming substances in the system under the condition of not adding a new medicament; so as to realize the purpose of zero emission and environmental pollution reduction of wastewater factories.
2. The utility model further processes partial produced water inside and outside the system to greatly reduce the ash water amount discharged to sewage treatment; the treated water can be used as sealing washing water for replenishing water of the pump, and a small amount of wastewater generated by the recovery device contains COD and ammonia nitrogen and can be discharged to a sewage treatment system.
3. The utility model discloses a special type nanometer filler adsorption technology and special type membrane coupling technique realize adsorbing the hardness of aquatic under the high temperature to resolve at normal atmospheric temperature, realize full process automation operation, adapt to higher hardness waste water treatment.
4. The utility model discloses can effectively reduce calcium magnesium ion content in the system, improve system's quality of water, delay the pipeline scale deposit and make system's resistance obviously descend, realize the long period operation of gasifier, solve the great phenomenon of the high system water supply of production consumption.
5. The desorption waste liquid discharge pipe in the system is communicated with a regeneration liquid recovery device, and the regeneration liquid recovery device is internally provided with a desorption waste liquid discharge pipeThere is a membrane separation structure. The analytic waste liquid is high-hardness salt-containing waste water, and strong brine after membrane separation and concentration is directly introduced into CO2Adjusting the pH value with sodium hydroxide, carrying out filter pressing, drying and packaging on the precipitate to create new economic benefit, conveying the filtrate to a regeneration tank, conveying the filtrate to a nano filler absorber through a regeneration pump for purification, and conveying the purified filtrate to an ash water recovery tank for recycling after purification.
6. The total hardness (calcium carbonate) of the water treated by the system is less than or equal to 100mg/L, the turbidity is less than or equal to 5NTU, and the water returns to a gasification grey water system for recycling.
Drawings
FIG. 1 is a schematic diagram of the overall structure of the system of the present invention;
FIG. 2 is a schematic diagram showing the specific connection of the backwash module of the multi-media filter of the present invention;
fig. 3 is a schematic diagram of the connection of the nanofiller adsorber of the present invention.
Detailed Description
The present invention will be further described with reference to the following specific embodiments. The following examples are intended to illustrate the invention and are not intended to limit the scope of the invention.
As shown in fig. 1-3, a gasified grey water hardness removal system comprises a settling tank 1, a new grey water tank 2, a plurality of multi-media filters 3 operating in parallel, a plurality of nano-filler adsorbers 4 operating in parallel, an auxiliary desorption unit and a grey water recovery tank 5 which are sequentially communicated; the ash water of the slag and ash water unit circulates to a settling tank 1 and then overflows to a new ash water tank 2, the ash water is sent to a multi-medium filter 3 and a nano filler absorber 4 through a hardness removing water pump 21 to remove calcium and magnesium ions in the ash water, and the qualified ash water is sent to an ash water recycling tank 5 and then is recycled to the system for further utilization. The settling tank 1 is used for preliminarily separating solid from liquid of raw ash water; the bottom of the settling tank 1 is provided with a settling tank underflow pump 11 which conveys solid substances such as slurry and the like at the bottom of the settling tank 1 to a filter press.
The new ash tank 2 is used for collecting the overflow clear liquid of the settling tank 1; the new ash tank 2 is used for collecting the overflow clear liquid of the settling tank 1; and the overflow clear liquid is sent to the multi-media filter 3 through the hard water removal pump 21, and the multi-media filter 3 is used for removing colloids and suspended matters in water, so that the water inlet requirement of the adsorption device is ensured. In the implementation, the multi-media filter 3 is filled with two kinds of quartz sand with different specifications, the filling height of the quartz sand with large particles at the bottom is about 0.5 m, the filling height of the quartz sand with small particles at the upper part is about 1.5 m, and in the implementation example, 8 sets of multi-media filters 3 are arranged in the system and run in parallel.
The multi-media filter 3 comprises a first water inlet pipe 31 communicated with the new ash water tank 2 and arranged at the upper part of the multi-media filter 3, and a first water outlet pipe 32 arranged at the lower part of the multi-media filter 3, wherein a hardness removing water pump 21 is arranged on the first water inlet pipe 31 and used for pumping the ash water in the new ash water tank 2 to the multi-media filter 3, a first water inlet valve 31a is correspondingly arranged on the first water inlet pipe 31, and a first water outlet valve 32a is correspondingly arranged on the first water outlet pipe 32.
The multi-media filter 3 is further provided with a backwashing module, the backwashing module comprises a backwashing discharge pipe 33 and a first discharge pipe 34 which are arranged at the top of the multi-media filter 3, and a forward washing discharge pipe 35 and an air inlet pipe 36 which are arranged at the bottom of the multi-media filter 3, a backwashing discharge valve 33a is correspondingly arranged on the backwashing discharge pipe 33, the first discharge pipe 34 is provided with a first exhaust valve 34a, the forward washing discharge pipe 35 is provided with a forward washing discharge valve 35a, and the air inlet pipe 36 is provided with an air inlet valve 36 a.
As shown in figure 2, when the water inlet and outlet pressure difference of the single set of the multi-medium filter 3 is more than 0.2Mpa or the running time is more than 8 hours, the single set of the multi-medium filter needs to be backwashed. Performing backwashing according to the following steps:
the first water inlet valve 31a of the multimedia filter 3 is closed, then the backwashing discharge valve 33a of the multimedia filter 3 is opened, after 3 minutes, the first water outlet valve 32a of the multimedia filter 3 is closed, then the forward washing discharge valve 35a and the exhaust valve of the multimedia filter 3 are opened, and after 3 minutes of water discharge, the forward washing discharge valve 35a and the first exhaust valve 34a are closed. The air inlet valve 36a of the multimedia filter 3 is opened, and 5 minutes later, the air inlet valve 36a is closed. And 5-10 minutes after the first water outlet valve 32a of the multimedia filter 3 is opened, the first water outlet valve 32a and the backwashing discharge valve 33a are closed. And opening a first water inlet valve 31a, a forward washing discharge valve 35a and a first exhaust valve 34a of the multi-media filter 3, closing the first exhaust valve 34a after the first exhaust valve 34a discharges water, opening a first water outlet valve 32a of the multi-media filter 3 after 2 minutes, closing the forward washing discharge valve 35a, putting into operation or standby, discharging a backwash liquid to a collection pool 8, and conveying the backwash liquid to the settling tank 1 through a grey water recovery pump 81 for further recycling.
The nano-filler adsorber 4 is used for adsorbing calcium and magnesium ions in the ash water at high temperature; in the embodiment, the nanofiller 4 is provided with 5 sets of parallel operating adsorbers, specifically, the nanofiller 4 is filled with about 8 tons of nano-resin particles, the nanofiller 4 is provided with an adsorbent inlet and outlet pipe 49, and the adsorbent inlet and outlet pipe 49 is used for renewing the adsorbent particles.
The nano-filler adsorber 4 comprises a second water inlet pipe 41 communicated with the multi-media filter 3 and arranged at the upper part of the nano-filler adsorber 4, and a second water outlet pipe 42 arranged at the lower part of the nano-filler adsorber 4, wherein a second water inlet valve 41a is correspondingly arranged on the second water inlet pipe 41, and a second water outlet valve 42a is correspondingly arranged on the second water outlet pipe 42.
The nano-filler adsorber 4 is provided with an analysis module, the analysis module comprises a regenerated analysis liquid inlet pipe 43 arranged at the lower part of the nano-filler adsorber 4 and an analysis waste liquid discharge pipe 44 arranged at the upper part of the nano-filler adsorber 4, and a regenerated analysis liquid inlet valve 43a and an analysis waste liquid discharge valve 44a are correspondingly arranged on the regenerated analysis liquid inlet pipe 43 and the analysis waste liquid discharge pipe 44 respectively; the device is characterized by further comprising a backwashing water inlet pipe 45 and a forward washing sewage pipe 46 which are arranged at the bottom of the nano filler adsorber 4, and a backwashing sewage pipe 47 and a second exhaust pipe 48 which are arranged at the top of the nano filler adsorber 4, wherein a backwashing water inlet valve 45a is correspondingly arranged on the backwashing water inlet pipe 45, a forward washing sewage valve 46a is arranged on the forward washing sewage pipe 46, a backwashing sewage valve 47a is arranged on the backwashing sewage pipe 47, and a second exhaust valve 48a is arranged on the second exhaust pipe 48.
And after the adsorption saturation of the adsorption device, the adsorption device is isolated from the adsorption system, the desorption device is used for desorbing the adsorbent to recover the adsorption performance of the adsorbent, and after the adsorbent is recovered, the adsorbent is put into the system for recycling.
As shown in FIG. 3, when the hardness of the effluent of the single nano-filler adsorber 4 is greater than 100mg/L or the operation time is greater than 4 hours, the desorption regeneration treatment is required. The regeneration treatment is carried out according to the following steps:
and (3) closing a second water inlet valve 41a and a second water outlet valve 42a of the nano adsorber, firstly opening a backwashing blowdown valve 47a of the nano adsorber, then opening a backwashing water inlet valve 45a, and closing the backwashing water inlet valve 45a and the backwashing blowdown valve 47a after 3 minutes. And opening a forward washing blowdown valve 46a and a second exhaust valve 48a of the nano-adsorber to exhaust the water in the nano-adsorber. Opening a regeneration analysis liquid inlet valve 43a of the nano adsorber, starting a regeneration pump 71 to fill water into the nano adsorber, opening a nano adsorber analysis waste liquid discharge valve 44a when the water level of the nano adsorber rises to the middle of a first sight glass, circulating for 20 minutes, supplementing the regeneration analysis liquid with the concentration of 10%, keeping the regeneration analysis liquid level inside the nano adsorber at the sight glass, analyzing for 40-45 minutes, stopping the regeneration analysis liquid, continuing filling water into the nano adsorber, replacing for 30-45 minutes, and stopping the regeneration pump 71 for use or standby.
The desorption device is used for storing desorption liquid, and the desorption liquid is pumped into the nanofiller adsorber 4 through a pipeline and is used for regenerating and desorbing the adsorbent. The regeneration analysis liquid inlet pipe 43 is communicated to a regeneration analysis device, and the regeneration analysis device is provided with 1 set and runs intermittently.
The analytic waste liquid discharge pipe 44 is communicated to the analytic liquid recovery processing device 6, the analytic liquid recovery processing device 6 is used for recovering and processing the analytic waste liquid, and a membrane separation structure is arranged in the analytic liquid recovery processing device 6, and the membrane separation structure at least comprises an ultrafiltration membrane, a nano-membrane and a reverse osmosis membrane. The analytic waste liquid is high-hardness salt-containing waste water, and strong brine after membrane separation and concentration is directly introduced into CO2Adjusting the pH value of the precipitate with sodium hydroxide, performing filter pressing, drying, packaging and selling the precipitate, and opening up new economic benefits. And (3) conveying the filtrate to a regeneration tank 7, conveying the filtrate to a nano filler adsorber 4 through a regeneration pump 71 for purification, and conveying the purified filtrate to an ash water recovery tank 5 for recycling.
The grey water recovery tank 5 is used for collecting the purified grey water and recycling the grey water to the system for further utilization.
In the embodiment, the multi-media filter 3, the nano-filler adsorber 4 and the regeneration analysis device in the system are all provided with a manual/automatic operation function, and are controlled by a PLC (programmable logic controller) cabinet during automatic control, and are divided into a pretreatment sub-control station, a nano-filler adsorption sub-control station and a regeneration analysis sub-control station, so that the whole system realizes full-automatic operation, and realizes respective functions of automatic/manual control and the like.
The main technical indexes are as follows:
1) design requirements of water inlet process indexes of ash water treatment new process device (see Table 1)
2) Acceptance criteria for effluent process indexes of ash water treatment new process device (see Table 2)
It is right to combine the embodiment the utility model discloses benefit and prospect carry out the analysis:
and (3) benefit analysis:
since the device operates, the operation and the generated cost benefit are comprehensively compared, (note: F represents the cost, and R represents the economic benefit cost), and the following summary is made:
annual plant operating cost
(1) Electric charge
The annual running time of the device is calculated according to 300 days, the device runs discontinuously, the device runs for 4 hours every day, the electricity consumption is 95 kilowatts every hour, and the electricity fee is calculated according to the following steps: and when the electricity consumption is calculated by 0.63 yuan/kilowatt hour, the annual running electricity charge is as follows:
f =300 × 4 × 95 × 0.63/10000=7.182 (ten thousand yuan/year)
(2) Cost of main consumables
The ultrafiltration membranes are replaced according to the service life of 3 years, 8 ultrafiltration membranes are arranged in the system, and the annual cost is as follows if each ultrafiltration membrane is calculated according to 15000 yuan:
f15000 × 8/3/10000 ═ 4 (ten thousand yuan per year)
The service life of nanofiltration is 3-5 years, we replace the nanofiltration membrane once according to 3 years, the system has 36 special nanofiltration membranes, each nanofiltration membrane has 12000 yuan per root, and the annual cost is as follows:
f =12000 × 36/3/10000=14.4 (ten thousand yuan/year)
The service life of the reverse osmosis membrane is 3-5 years, the reverse osmosis membrane is replaced once according to 3 years, the system special reverse osmosis membrane is 18, and the system reverse osmosis membrane is 5000 yuan/root, so the annual cost is as follows:
f = 5000X 18/3/10000=3 (ten thousand yuan/year)
The loss of the nano adsorbent is calculated according to 5% per year, the unit price of each ton of the adsorbent is 65000 yuan/ton, the filling amount of the system adsorbent is 32 tons, and the annual cost is as follows:
f =32 × 65000 × 5%/10000=10.4 (ten thousand yuan/year)
(II) chemical consumption cost:
the industrial salt is calculated according to the market price of 350 yuan/ton, the consumption of the industrial salt is calculated according to the consumption of 0.25kg of salt per ton of grey water, 300 tons of grey water are treated per hour, and the annual cost is as follows:
f =300 × 24 × 300 × 0.25/1000 × 350/10000=18.9 (ten thousand yuan/year)
(III) annual operating cost:
the annual operating cost of the device is as follows:
f =7.182+4+14.4+3+10.4+18.9=54.882 (ten thousand yuan/year)
(IV) expected economic benefits
The sewage treatment cost is as follows: before the project is implemented, in order to control the hardness of the system, the wastewater is discharged into a built sewage treatment plant, 80 tons of wastewater are discharged per hour by 2 gasification furnaces, the discharge amount of the wastewater is reduced to 50 tons after the project is implemented, the wastewater treatment cost is calculated according to 4.5 yuan per ton, and 4 gasification furnaces jointly generate emission reduction benefit cost:
r1 ═ 4.5 × 300 × 24 × (80-50) × 2/10000=194.4 (ten thousand yuan/year)
Water cost of desalted water: after the pollution discharge is reduced, the consumption of desalted water is correspondingly reduced, the desalted water amount is reduced by 30 tons per hour, and the desalted water benefit cost is reduced according to 5.0 yuan per ton:
r2=30 × 300 × 24 × 5/10000=108 (ten thousand yuan/year)
The cost of the medicament is reduced: the cost for reducing the scale inhibition dispersant is calculated according to 35 percent, the conventional statistical average value of the aerospace furnace industry is used for estimation, and the annual medicament cost is calculated according to 300 ten thousand yuan, so that the medicament benefit cost is reduced:
r2=300 × 35% =105.00 (ten thousand yuan/year)
Expected direct economic benefit of the plant:
r194.4 +108+105-54.882 ═ 352.518 (ten thousand yuan/year)
(V) social benefits
The adoption of the nano-filler adsorption technology and the special membrane coupling technology realizes the adsorption of calcium and magnesium ions in the ash water at high temperature, improves the water quality, delays the scaling, reduces the sewage treatment capacity, and reduces the addition of external agents, so that the economic efficiency and the environmental protection performance are more obvious.
From the economic analysis of the project, the project investment solves the problem of wastewater treatment, has certain economic benefit, is an environment-friendly project with expected economic benefit, and can realize the resource utilization of wastewater.
Application range, prospect and market analysis:
the technology solves the problem of ash water treatment which troubles the coal gasification industry for many years. The process is simple, the flow is short, the equipment is few, the automation degree is high, the remote intelligent maintenance and management can be realized, and the system stability is improved. The technology solves the problems of scaling and blockage caused by high hardness of the gasification furnace grey water system, and the operation cost of the system is lower without adding new medicament to the system during operation. The sewage discharge amount after the grey water treatment is reduced, the sewage treatment difficulty is reduced, the production and operation cost of the sewage is further reduced, the wastewater is recycled, the supplementary water amount of desalted water is greatly saved, and the raw water consumption is further saved; meanwhile, the content of substances such as salt, COD (chemical oxygen demand), ammonia nitrogen and the like in the grey water system can be reduced, and the hardness of water can be reduced, so that the project is worthy of popularization and application in the grey water treatment system.
Claims (7)
1. A gasification grey water hardness removal system is characterized by comprising a settling tank, a new grey water tank, a plurality of multi-medium filters which operate in parallel, a plurality of nano-filler adsorbers which operate in parallel, an auxiliary analysis unit and a grey water recovery tank which are sequentially communicated;
the settling tank is used for preliminarily separating solid from liquid of the raw ash water;
the new ash tank is used for collecting overflow clear liquid of the settling tank;
the multi-medium filter is used for removing colloids and suspended matters in water and ensuring the water inlet requirement of the adsorption device;
the nano filler adsorber is used for adsorbing calcium and magnesium ions in the ash water at high temperature;
the auxiliary analysis unit comprises an analysis device and an analysis liquid recovery processing device, the analysis device is used for storing analysis liquid, pumping the analysis liquid into the nanofiller adsorber through a pipeline and regenerating and analyzing the adsorbent, and the analysis liquid recovery processing device is used for recovering and processing analysis waste liquid;
and the grey water recovery tank is used for collecting the purified grey water and recycling the grey water to the system for further utilization.
2. The gasification grey water hardness removal system of claim 1, wherein the multi-media filter is filled with silica sand and the adsorbent inside the nanofiller adsorber is a nano resin particle.
3. The system for removing hardness from gasified grey water according to claim 1, wherein the multi-media filter comprises a first water inlet pipe connected to the new grey water tank and disposed at the upper part of the multi-media filter, and a first water outlet pipe disposed at the lower part of the multi-media filter, the first water inlet pipe is provided with a hardness-removing water pump for pumping the grey water in the new grey water tank into the multi-media filter, the first water inlet pipe is correspondingly provided with a first water inlet valve, and the first water outlet pipe is correspondingly provided with a first water outlet valve.
4. The gasified grey water hardness removal system of claim 3, wherein the multi-media filter is further provided with a back washing module, the back washing module comprises a back washing discharge pipe and a first discharge pipe which are arranged at the top of the multi-media filter, and a forward washing discharge pipe and an air inlet pipe which are arranged at the bottom of the multi-media filter, the back washing discharge pipe is correspondingly provided with a back washing discharge valve, the first discharge pipe is provided with a first exhaust valve, the forward washing discharge pipe is provided with a forward washing discharge valve, and the air inlet pipe is provided with an air inlet valve.
5. The gasified grey water hardness removal system of claim 1, wherein the nanofiller adsorber comprises a second inlet pipe connected to the multimedia filter and disposed at an upper portion of the nanofiller adsorber, and a second outlet pipe disposed at a lower portion of the nanofiller adsorber, and wherein the second inlet pipe is correspondingly provided with a second inlet valve, and the second outlet pipe is correspondingly provided with a second outlet valve.
6. The gasified grey water hardness removal system of claim 5, wherein the nanofiller adsorber is provided with a desorption module comprising a regeneration desorption liquid inlet pipe disposed at a lower portion of the nanofiller adsorber and a desorption waste liquid outlet pipe disposed at an upper portion of the nanofiller adsorber, and wherein the regeneration desorption liquid inlet pipe is provided with a regeneration desorption liquid inlet valve and the desorption waste liquid outlet pipe is provided with a desorption waste liquid outlet valve; the device is characterized by further comprising a backwashing water inlet pipe and a forward washing blow-off pipe which are arranged at the bottom of the nano filler adsorber, and a backwashing blow-off pipe and a second exhaust pipe which are arranged at the top of the nano filler adsorber, wherein a backwashing water inlet valve is arranged on the backwashing water inlet pipe correspondingly, a forward washing blow-off valve is arranged on the forward washing blow-off pipe, a backwashing blow-off valve is arranged on the backwashing blow-off pipe, and a second exhaust valve is arranged on the second exhaust pipe.
7. The gasified grey water hardness removal system of claim 6, wherein the desorption waste liquid discharge pipe is communicated with a desorption liquid recovery processing device, and a membrane separation structure is arranged in the desorption liquid recovery processing device and at least comprises an ultrafiltration membrane, a nano membrane and a reverse osmosis membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021242700.9U CN212450860U (en) | 2020-06-30 | 2020-06-30 | Gasification buck removes hard system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021242700.9U CN212450860U (en) | 2020-06-30 | 2020-06-30 | Gasification buck removes hard system |
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