CN100548911C - A kind of process for treating oil-containing sludge - Google Patents
A kind of process for treating oil-containing sludge Download PDFInfo
- Publication number
- CN100548911C CN100548911C CNB2007101454603A CN200710145460A CN100548911C CN 100548911 C CN100548911 C CN 100548911C CN B2007101454603 A CNB2007101454603 A CN B2007101454603A CN 200710145460 A CN200710145460 A CN 200710145460A CN 100548911 C CN100548911 C CN 100548911C
- Authority
- CN
- China
- Prior art keywords
- mud
- treatment
- flocculation
- sludge
- drying
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Treatment Of Sludge (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The present invention relates to a kind of process for treating oil-containing sludge, comprise the concentration step, flocculation-centrifuge dehydration step and drying and other treatment step, wherein: mud is disposed to the thickened sludge transport pipe after gravity settling concentrates, to the thickened sludge transport pipe, add flocculation agent from drug dissolving tank simultaneously, make flocculation agent and thickened sludge hybrid reaction, mud after flocculation is transported in the centrifuge, mud after centrifuge dehydration is delivered to the vapo(u)r blasting sludge treating system and carries out drying and other treatment, and the mud outward transport after the drying and other treatment further fully utilizes.The present invention further comprises the fixing of repugnant substance and removes step.Each treatment step of aforesaid method continuously and cooperatively interact into as a wholely has that treatment effect is good, broad spectrum, non-secondary pollution, can reclaim advantages such as petroleum resources, energy consumption is low, running cost is low.
Description
Technical field
The present invention relates to handle the method for oil play oil-containing solids refuse, be specifically related to a kind of process for treating oil-containing sludge.
Background technology
Oil field, normal mud, the heavy mud in jar end and the refinery factory oil-containing " three mud " (oil trap bed mud, dissolved air floatation pond scum silica frost, petroleum tank bed mud) etc. of landing of petroleum refinery's oil movement and storage system are referred to as oily sludge with them.Material foul smellings such as the hydrogen sulfide that contains in these mud, thio-alcohol, amine flavor and toxicity if directly enter in the physical environment, can cause bigger pollution to surrounding soil, water body and vegetation.A large amount of petroleum resources have also been wasted simultaneously.Therefore, no matter be to consider from environment protection or from the angle that reclaims the energy, all must handle oily sludge.
Tradition oily sludge tupe is: mud modulation-centrifuge dehydration-burning, French, German petroleum chemical enterprise adopts the mode of burning more, at home, still has a lot of refinerys to adopt burning disposal.Although oily sludge almost can all be removed multiple harmful substances through after the burning disposal,, burning sludge needs a large amount of diesel oil or sump oil, and heat mostly is not recovered utilization again, and cost is very high, invest also very big, and in the burning process also with serious atmospheric pollution.
Hot washing method, solvent extration, solid-liquid isolation method, chemical demulsification method, centrifuge dehydration and microorganism treatment etc. have been reported in recent years in succession, the part oil play sludge treatment facility that also started.For example U.S. Pat 6673231A introduce to use pyrogen oil flushing jar bed mud to distill to handle the purpose that reaches clearly jar with sludge treatment two aspects again, but a large amount of pyrogen oil of this arts demand.WO92/04424 has introduced and has adopted a series of vaporization/condensation art breading mud, does not handle the high mud of oleaginousness but be suitable for.
Owing on treatment process, also there are many problems, at present still not having method or the equipment that a kind of cost is low, technology is really up to the mark can apply, direct landfill or construction storage pool are deposited temporarily and are still the first-selected treatment process that present most of oil play is handled oily sludges behind natural drying, the oily sludge of a large amount of landfills has not only wasted petroleum resources, but also has polluted the landfill yard surrounding enviroment.
Summary of the invention
The object of the present invention is to provide a kind of economy, process for treating oil-containing sludge effective, applied widely.
According to a kind of process for treating oil-containing sludge of the present invention, comprise the concentration step, flocculation-centrifuge dehydration step and drying and other treatment step, wherein: in the concentration step, the oily sludge that will compile or collect in the sludge sump is promoted to the mud concentration tank through the mud lift pump, further deviate from part free-water wherein after mud is handled by gravity settling in concentration tank, the reaction times is 2～60 hours, and the mud waste water after concentrating enters wastewater treatment field; In the flocculation-centrifuge dehydration step, thickened sludge after concentration is transported to the thickened sludge transport pipe, to the thickened sludge transport pipe, add flocculation agent from drug dissolving tank simultaneously, make flocculation agent and thickened sludge hybrid reaction, reaction times is 5～60 seconds, and the mud after flocculation is transported in the centrifuge, and the mud after the dehydration is delivered to drying and other treatment equipment and carries out drying and other treatment, the oil that reclaims after the oily water separation is stored in the oil tank, and the waste water after the separation enters wastewater treatment field; In the drying and other treatment step, after mud mud cake after flocculation-centrifugal dehydration treatment or body refuse are delivered to the hopper of vapo(u)r blasting sludge treating system, under the feeder effect, enter treatment chamber, mud mud cake or body refuse are pulverized under the high temperature and high speed vapo(u)r blasting, oil content and moisture content are evaporated out simultaneously, pulverized fine particle enters cyclonic separator together with steam, realize separating of steam and solid particulate by cyclonic separation, solid particulate directly enters the residue accumulator tank, steam enters gun barrel and realizes oily water separation after the condenser cooling, the mud outward transport after the drying and other treatment further fully utilizes.
According to a kind of process for treating oil-containing sludge of the present invention, can further include step in the described concentration step to the mud heating, the mud Heating temperature is 20～60 ℃.
According to a kind of process for treating oil-containing sludge of the present invention, the flocculation agent that is adopted in the described flocculation treatment step includes but not limited to PAC, PFC, Tai-Ace S 150 and CPAM, preferred CPAM, its molecular weight is 800～1,200 ten thousand, the dosage of the preferred relative mud of CPAM is 80-200mg/L.
According to a kind of process for treating oil-containing sludge of the present invention, can further include the step of adjusting flocculation reaction pH value in the described flocculation treatment step, selecting the pH value is 2～7, is preferably 7.
According to a kind of process for treating oil-containing sludge of the present invention, the temperature of high-temperature steam is 500-600 ℃ in the described drying and other treatment step.
According to a kind of process for treating oil-containing sludge of the present invention, it further comprises throws in the step that basic agent fixes and remove the sulfur-containing foul material in oily sludge, and described basic agent includes but not limited to NaOH, Na
2CO
3, NaHCO
3, Ca (OH)
2, CaO, Ca (HCO
3)
2Or its mixture, described basic agent addition is that mud per ton is thrown in 1～8 kilogram.
According to above-mentioned process for treating oil-containing sludge of the present invention, it provides a kind of and has all had the scalable treatment process of positive effect at various oily sludges, with respect to adopting the technical solution of burning, burying to have the more treatment effect of system in the prior art separately.
Because the present invention has adopted and has concentrated, flocculation-centrifugal and the technical solution that drying and other treatment matches, with respect to wherein a kind of treatment process of independent employing, its greasy filth treatment effect is better.
After concentrating, moisture percentage in sewage sludge is reduced to about 97%-98% by about 99%, and reduction in bulk is more than 50%.Use whizzer, be equipped with flocculation agent, can reduce to 65%～70% through the water ratio of dense mud after the centrifuge dehydration.Drying and other treatment partly adopts oily sludge superheated steam inject process technology.The residue oil length is minimum after handling reaches 0.08%, and actual oil length is controlled at below 5%.Do not contain heavy metal in the refiltered oil and removed most of sulphur, the Water in oil rate can reduce to 0.12%, and the water ratio of residue can be reduced to below 1%.
Can reach following beneficial effect by technical scheme of the present invention:
1. method proposed by the invention can satisfy the sludge treatment requirement of various trait, and the treatment effect of the mud that mud, oil-sand or different properties crude oil that different production links such as oil, jar bed mud produce forms is all fine to landing.
2. compared with prior art, have that treatment effect is good, broad spectrum, non-secondary pollution, can reclaim characteristics such as petroleum resources, energy consumption is low, running cost is low.
3. handle controlled minimum the reaching of residue oil length＜0.3% later, direct landfill, and residual organic mainly is some larger molecular organicses that have been carbonized in the residue, does not generally have environmental toxicity and bio-toxicity.Three mud dry powders combustion heat value after testing can mix in the coal and burn greater than 3600 kcal/kg, and calorific value can utilize.
4. that reclaims is oily pure, does not contain heavy metal and has removed most of sulphur, and the Water in oil rate can reduce to 0.12%.
5. energy consumption is low.Make fuel with diesel oil or recovery crude oil, utilize pipeline steam to make vapour source, Actual Burnoff only is 6-8L/h., and power consumption only is 2.8kWh.
Require emphasis, those skilled in the art should be understandable that, in embodiment of the present invention, each treatment step is continuously and cooperatively interacts into as a whole, being provided be mutually related turnover pipeline or charging and discharging mouth between each treatment scheme and even each equipment, guaranteeing that oily sludge such as three mud directly becomes Powdered solid-state by the liquid state of moisture＞98% after whole process is handled.Adopt the situation of a certain processing mode separately for the entire treatment flow process being isolated come, the combination of its effect is far away from the obtainable technique effect of overall flow.For example, adopt separately the combination that concentrates or adopt separately flocculation-centrifugal or adopt drying and other treatment separately the effect that is obtained be can't reach the present invention's process for treating oil-containing sludge required for protection obtainable above-mentioned technique effect.
Description of drawings
Fig. 1 is the main schematic flow sheet of method for sludge treatment of the present invention.
Fig. 2 is a flocculation-centrifuge dehydration schema.
Fig. 3 is a vapo(u)r blasting treatment system schematic flow sheet.
Embodiment
To a preferred embodiment of the present invention will be described in detail, should be appreciated that following embodiment only is used for clearer, the detailed the present invention that understands with reference to the accompanying drawings, and be not used in protection scope of the present invention is limited to following specific embodiment.
Embodiment 1
A kind of process for treating oil-containing sludge according to embodiments of the invention 1 comprises the concentration step, flocculation-centrifuge dehydration step and drying and other treatment step, wherein:
In the concentration step, the oily sludge that will compile or collect in the sludge sump is promoted to the mud concentration tank through sludge pump, further deviate from part free-water wherein after mud is mainly handled by gravity settling in concentration tank, reaction times is 2～60 hours, and the mud waste water after concentrating enters wastewater treatment field.
Through after the concentration, moisture percentage in sewage sludge can be reduced to about 97%-98% by about 99%, and reduction in bulk is more than 50%.
Can further include the step to mud heating in the concentration step of the process for treating oil-containing sludge of present embodiment, mud is heated to 20～60 ℃, to guarantee that the reaction of mud and medicament reaches good effect in the follow-up flocculation treatment process.
In the flocculation-centrifuge dehydration step, thickened sludge after concentration is transported to the thickened sludge transport pipe, to the thickened sludge transport pipe, add flocculation agent from drug dissolving tank simultaneously, make flocculation agent and thickened sludge hybrid reaction, 5～60 seconds reaction times, this reaction process is just to have finished in the process that thickened sludge is carried in the thickened sludge transport pipe basically, mud after flocculation is transported in the centrifuge, mud after the dehydration is delivered to storage basin, carry out drying and other treatment in order to drying and other treatment equipment, the oil that reclaims after the oily water separation is stored in the slop oil tank, and the waste water after the separation enters wastewater treatment field.
Mud after centrifugal has been realized oil, water, mud three phase separation.
The flocculation agent that is adopted in the flocculation treatment step of the process for treating oil-containing sludge of present embodiment includes but not limited to PAC (polymerize aluminum chloride), PFC (poly-ferric chloride), Tai-Ace S 150 and polyacrylamide series (CPAM).Wherein, preferred flocculation agent CPAM, its molecular weight is 800～1,200 ten thousand, the dosage of the preferred relative mud of CPAM is 80-200mg/L.
Can further include the step of adjusting flocculation reaction pH value in the flocculation treatment step of the process for treating oil-containing sludge of present embodiment, selecting the pH value is 2～7, and preferred pH value is 7.
In the drying and other treatment step, the mud mud cake (slag) after flocculation-centrifugal dehydration treatment is delivered to the vapo(u)r blasting sludge treating system and carries out drying and other treatment, and dewatered sludge further fully utilizes through the outward transport of mud outward transport equipment.
Its concrete steps are: after the mud mud cake (slag) after flocculation-centrifugal dehydration treatment is delivered to the hopper of vapo(u)r blasting sludge treating system, enter treatment chamber through feeder, mud mud cake (slag) is pulverized under the high temperature and high speed vapo(u)r blasting, oil content and moisture content are evaporated out simultaneously, pulverized fine particle enters cyclonic separator together with steam, realize separating of steam and solid particulate by cyclonic separation, solid particulate directly enters the residue accumulator tank, and steam enters gun barrel and realizes oily water separation after the condenser cooling.
Adopted the vapo(u)r blasting sludge treating system to carry out drying and other treatment in the drying and other treatment step of the process for treating oil-containing sludge of present embodiment, wherein the vapo(u)r blasting sludge treating system mainly comprises steam generating system, feed system, sludge drying treatment system, vapour/solid separation system and Controlling System.
Steam generating system
Steam generating system comprises conventional steam boiler and superheater two portions, and conventional steam boiler can directly be bought the commodity boiler.The principle of work of superheater is to adopt airtight helix tube type heating system, is fuel with liquefied petroleum gas (LPG) or diesel oil, directly sprays into flame to the spiral tube center steam is heated up, by control fuel and flow control vapor temperature.During for employing vapo(u)r blasting treatment system, the temperature of steam is the important factor that must consider, shows according to experiment, and to most mud samples, 500 ℃～600 ℃ (optimum 550 ℃) are comparatively suitable treatment temps.
Feed system
Feed system is made up of hopper and feeder, and feeder is by electric motor driving, and the control of the controlled system of motor opens and closes according to setting chamber temperature.When temperature meets or exceeds the setting treatment temp, electric motor starting, beginning is sent into mud to the sludge drying treatment system.Mud and steam reaction meeting consumption of calorie cause temperature reduction in the sludge drying treatment system, and when sludge drying treatment system temperature was lower than design temperature, motor quit work, and no longer carried mud to the sludge drying treatment system.At this moment, sludge drying treatment system temperature can raise gradually, and until reaching design temperature, motor restarts work.
The sludge drying treatment system
The sludge drying treatment system comprises treatment chamber and vapor-nozzle, vapor-nozzle make steam relatively low pressure (＜0.5MPa) make vapo(u)r blasting speed reach subsonic speed or supersonic speed under the situation.Adopt a kind of jet pipe technology (Laval nozzle technology) that is widely used in missile propulsive plant and wind1 tunnel trial.The type jet pipe is made of two tapered tubes, and wherein front end is a collapsible tube, and the rear end is a convergent divergent channel.The forebody of jet pipe is to be contracted to a narrow larynx to the centre from large to small, and changing from small to big again after the narrow larynx expands outwardly.
The superheated steam steam flow is under the boiler pressure effect, further quicken through jet pipe, when entering the nozzle vapor pressure and be general boiler pressure, nozzle end gas flow velocity just can reach 2 overtone speed, (〉=500 ℃ of superheated steams, can reach 600 ℃) spray from special nozzle with ultra-high speed (above 2 Mach), carry out vertical collision with mud granule, mud granule is under the kinetic energy effect that superthermal gas heat energy and high speed are produced, liquid such as intragranular petroleum-type and water ooze out into particle surface from granule interior rapidly, and be evaporated rapidly, thereby liquid such as realization oil content separate with solid, reach quick-drying purpose.
Vapour/solid separation system
Under, the high speed steam flow effect superthermal at treatment chamber, admittedly mud has formed vapour/mix steam flow, the purpose of vapour/solid separation system will make solid separate from water and oil vapour exactly, and vapour/solid separation system adopts cyclonic separator.
The cyclonic separator structure comprises steam inlet pipe, upper shell, lower cone and central Steam Pipe etc., after the dust-laden gas enters cyclonic separator by steam inlet pipe, along the tangential direction of cylinder, makes circumferential motion from top to bottom.Particle is in the steam flow rotary course, and the centrifugal force that is subjected to is big, so gradually to the barrel motion, fall along wall behind the arrival barrel, discharges from cone.Steam steam flow after the purification from bottom to top rotates in the central shaft environs, after the discharge of top steam discharge pipe.
A kind of process for treating oil-containing sludge various processes to embodiments of the invention 1 is further detailed below.
The flocculation agent test
Different tests has been carried out in selection to flocculation agent in the flocculation treatment step of the process for treating oil-containing sludge of present embodiment, and concrete testing data is referring to table 1～6.
Polyacrylamide series (CPAM) to PAC, Tai-Ace S 150 and different molecular weight has been carried out floc test.Wherein, the dosage that inorganic flocculating agent is selected for use is 2000-3000mg/L, and experiment condition is 50 ℃ of following gentle agitation of constant temperature 3 minutes.The treatment effect of different inorganic flocculating agents sees Table 1.The dosage of CPAM is about 100mg/L, and the CPAM treatment effect of different molecular weight sees Table 2.
| Medicament | Mud g | Temperature ℃ | Settling time min | Dehydrating amount mL | Slag blanket oil length % | Oil reservoir solid content % |
| PAC | 20 | 50 | 30 | 6.0 | 20.7 | 9.6 |
| Al 2(SO 4) 3 | 20 | 50 | 30 | 4.0 | 22.5 | 8.9 |
| PFC | 20 | 50 | 30 | 3.5 | 23.1 | 7.9 |
The treatment effect of the different flocculation agents of table 1
| CPAM (molecular weight) | Temperature ℃ | Mud g | Water mL | De-oiling rate % | Dehydration rate % |
| 8,000,000 | 55 | 40 | 10 | 76.3 | 79.5 |
| 1,000 ten thousand | 55 | 40 | 10 | 79.2 | 83.8 |
| 1,200 ten thousand | 55 | 40 | 10 | 95.9 | 89.1 |
| 1,400 ten thousand | 55 | 40 | 10 | 63.5 | 60.9 |
The treatment effect of the CPAM of table 2 different molecular weight
From above-mentioned experimental result as can be seen, use PAC to handle and have certain effect, the treatment effect of different processing medicaments has certain general character, and promptly the upper strata all forms the water-in-oil system, and phase inversion has promptly taken place.In addition, also relevant with stirring intensity, stirring acutely then can not form.
The treatment effect of CPAM is best in the organic floculant, also chooses CPAM in the present embodiment its different dosages are investigated treatment effect, the results are shown in Table 3.Treatment effect was best when the dosage of mud was 80-200mg/L relatively.
| CPAM dosage (mg/L) | Mud g | Water mL | Temperature ℃ | Experimental phenomena |
| 30 | 40 | 10 | 30 | Sedimentation does not have water sepn to go out; Centrifugally can not realize three phase separation |
| 60 | 40 | 10 | 30 | Sedimentation has water sepn to go out; Centrifugally can realize three phase separation, but the water layer muddiness, the upper strata is a scum silica frost |
| 90 | 40 | 10 | 30 | Sedimentation has water sepn to go out; Centrifugally can realize three phase separation, there is a small amount of oil on the upper strata, and major part is a slag |
| 110 | 40 | 10 | 30 | Sedimentation has water sepn to go out; Centrifugally can realize three phase separation, there is a small amount of slag on the upper strata, and major part is an oil |
| 130 | 40 | 10 | 30 | Sedimentation has water sepn to go out; Centrifugally can realize three phase separation, the upper strata is pure oil |
| 140 | 40 | 10 | 30 | Sedimentation has water sepn to go out; Centrifugally can realize three phase separation, the upper strata is the slag of bulk |
| 150 | 40 | 10 | 30 | Sedimentation does not have water sepn to go out; Centrifugally can not realize three phase separation |
The treatment effect of the different dosages of table 3CPAM
Provided the data of the dehydration rate under the differing temps, de-oiling rate in the table 4, from testing data as can be seen, within 55 ℃, with the rising of temperature, dehydration rate, de-oiling rate raise gradually, when reaching 55 ℃, it is the highest that de-oiling rate, dehydration rate all reach, and is respectively 92.4% and 89.1%; Along with the rising of temperature, de-oiling rate, dehydration rate all descend to some extent when temperature surpasses 55 ℃.Take all factors into consideration factors such as energy consumption, optimal reaction temperature is selected in 40 ℃, handles getting final product under the normal temperature in summer, and winter is temperature a little.
| Temperature ℃ | Mud g | Water ml | CPAM3 dosage mg/L Mud | De-oiling rate % | Dehydration rate % |
| 25 | 40 | 10 | 104 | 67.6 | 80.7 |
| 40 | 40 | 10 | 104 | 90.3 | 85.3 |
| 55 | 40 | 10 | 104 | 95.9 | 89.1 |
| 65 | 40 | 10 | 104 | 59.7 | 60.2 |
| 75 | 40 | 10 | 104 | 61.1 | 50.9 |
| 85 | 40 | 10 | 104 | 20.3 | 10.6 |
Dehydration rate under table 4 differing temps, de-oiling rate
Sludge dewatering under acidic conditions, de-oiling rate all increase, but the amplitude that improves and little, and have increased the corrosion to equipment under the acidic conditions, and therefore, selecting the pH value is 7 to carry out flocculation treatment.Corresponding test-results is referring to table 5.
| The pH value | CPAM3 dosage mg/L | Temperature ℃ | Mud g | Water ml | Dehydration rate | The de-oiling rate |
| 2-3 | 104 | 40 | 40 | 10 | 98.7 | 95.5 |
| 4-5 | 104 | 40 | 40 | 10 | 93.6 | 91.8 |
| 6-7 | 104 | 40 | 40 | 10 | 95.9 | 89.1 |
| 8-9 | 104 | 40 | 40 | 10 | - | - |
| 10-11 | 104 | 40 | 40 | 10 | - | - |
Result under the different pH values of table 5
Result of study to stirring velocity shows that lower stirring velocity just can reach treatment effect preferably, and when stirring velocity was too high, treatment effect descended on the contrary.Therefore, present embodiment will add before flocculation agent is chosen in into whizzer.In a simultaneous test, before concentrating, add flocculation agent through the laggard whizzer that dewaters, need during this period of time about 2 days.In this process, concentrated poly-agglomerating mud floss and can merge again again and come, formed new more stable colloid and can't separate, even add flocculating aids again or other flocculation agents do not have positive effect yet.In the present embodiment, flocculation agent is directly added before whizzer,,, thereby can obtain best effect so medium enters flocculation fully behind the whizzer because the flocculation reaction process of mud only needed to finish for tens seconds.Table 6 has provided the aquifer yield under the different stirring velocitys.
| Stirring velocity shelves speed r/min | CPAM(NO 3) mg/L | Temperature ℃ | Mud g | Water ml | Aquifer yield ml |
| 30 | 104 | 40 | 40 | 10 | 19 |
| 60 | 104 | 40 | 40 | 10 | 24 |
| 90 | 104 | 40 | 40 | 10 | 22.7 |
| 120 | 104 | 40 | 40 | 10 | 13 |
| 150 | 104 | 40 | 40 | 10 | 6 |
Aquifer yield under the different stirring velocitys of table 6
In actual use, the drug dissolving tank supporting with whizzer just can reach flocculation agent and the requirement of mud blended, need not to increase whipping appts again.
Embodiment 2
Present embodiment has carried out further improvement to the process for treating oil-containing sludge among the embodiment 1, has increased the fixing of sulfur-containing foul material in the present embodiment and has removed step, and other technical process is identical with other aspects of embodiment 1.
The main repugnant substance that oily sludge produced is hydrogen sulfide and mercaptan.Sulfide content is generally all very high in " three mud " that Petrochemical Enterprises produces, cause in three mud treatment facilities and the place and peripheral hydrogen sulfide content very high, in three traditional mud treatment process, the operator that hydrogen sulfide causes poison even death incident occurs repeatedly.Sulfide in three mud is mainly by two sources, and the one, element sulphur is after processing in the processed crude oil, and a part enters sewage work with the form of sulfide, and finally enters in three mud; Another part sulfide comes from the sewage sulphate reducing bacteria to the reductive action of sulfate radical in the water.
Malodorous generation source is to locate between sludge sump, concentration tank, centrifugal dehydration treatment etc. in the three mud treating processess, therefore, present embodiment provides the fixing of a kind of sulfur-containing foul material and has removed step, and it can be applied to concentration, flocculation-steps such as processed processing respectively.
Present embodiment further provides the fixing of sulfur-containing foul material and has removed step, and be specially: delivering medicament in oily sludge, medicament are the mixture of alkali, comprising but be not limited to NaOH, Na
2CO
3, NaHCO
3, Ca (OH)
2, CaO, Ca (HCO
3)
2Or its mixture, the addition of medicament is that mud per ton is thrown in 1～8 kilogram, the sulfide reaction in medicament and three mud generates solid matter, stable existence under field conditions (factors).The solid matter that generates after centrifuge dehydration enters solid phase, enters the desiccation apparatus mummification through helix transporting device again, and this solid is retained in the dry powder after the mummification, is converted into the salt solid after calcination, can not produce new pollution to environment.
Fixing and removing step of the sulfur-containing foul material that present embodiment provided can be applied to concentration step and/or flocculation-dehydration process steps respectively.Be specially, in the concentration step, in concentration tank, throw in above-mentioned basic agent, concentration response in the time (2～60 hours) enough this basic agent react with repugnant substance in the mud.In addition, in flocculation process, also can when adding flocculation agent, add above-mentioned basic agent, make it with mud in the repugnant substance reaction with fixing and remove stench.
Present embodiment adopts a kind of chemical process that the sulfide in three mud is fixed, after the dosing reaction, sulfide is stably remained in the solid phase with sulphided form, greatly suppress the generation of hydrogen sulfide and overflow to loose, significantly reduce the working space hydrogen sulfide content, site test results shows, without jack works peripheries hydrogen sulfide content after the fixed three mud centrifuge dehydrations up to more than the 100PPM, reduce to about 5PPM through on-the-spot concentration of hydrogen sulfide after the fixed three mud centrifuge dehydrations, behind the supporting installation ventilation plant, concentration of hydrogen sulfide is reduced to about 0.4PPM.
Residue mixes and advances heat power plant's burning in the coal after handling, and realizes the recycling and the zero release of " three mud ".
Claims (11)
1. a process for treating oil-containing sludge comprises the concentration step, flocculation-centrifuge dehydration step and drying and other treatment step, wherein:
In the concentration step, the oily sludge that will compile or collect in the sludge sump is promoted to the mud concentration tank through the mud lift pump, further deviate from part free-water wherein after mud is handled by gravity settling in concentration tank, reaction times is 2～60 hours, and the mud waste water after concentrating enters wastewater treatment field;
In the flocculation-centrifuge dehydration step, thickened sludge after concentration is transported to the thickened sludge transport pipe, to the thickened sludge transport pipe, add flocculation agent from drug dissolving tank simultaneously, make flocculation agent and thickened sludge hybrid reaction, reaction times is 5～60 seconds, and the mud after flocculation is transported in the centrifuge, and the mud after the dehydration is delivered to drying and other treatment equipment and carries out drying and other treatment, the oil that reclaims after the oily water separation is stored in the oil tank, and the waste water after the separation enters wastewater treatment field;
In the drying and other treatment step, after mud mud cake after flocculation-centrifugal dehydration treatment or body refuse are delivered to the hopper of vapo(u)r blasting sludge treating system, under the feeder effect, enter treatment chamber, mud mud cake or body refuse are pulverized under the high temperature and high speed vapo(u)r blasting, oil content and moisture content are evaporated out simultaneously, pulverized fine particle enters cyclonic separator together with steam, realize separating of steam and solid particulate by cyclonic separation, solid particulate directly enters the residue accumulator tank, steam enters gun barrel and realizes oily water separation after the condenser cooling, the mud outward transport after the drying and other treatment further fully utilizes.
2. method according to claim 1 is characterized in that, comprises further also in the described concentration step that the mud Heating temperature is 20～60 ℃ to the step of mud heating.
3. method according to claim 1 is characterized in that, the flocculation agent that is adopted in described flocculation-centrifugal dehydration treatment step is PAC, PFC, Tai-Ace S 150 or CPAM.
4. method according to claim 3 is characterized in that, described flocculation agent is CPAM, and the dosage of the relative mud of CPAM is 80-200mg/L.
5. according to claim 3 or 4 described methods, it is characterized in that described CPAM molecular weight is 800～1,200 ten thousand.
6. method according to claim 1 is characterized in that, also further comprises the step of adjusting flocculation reaction pH value in described flocculation-centrifugal dehydration treatment step, and selecting the pH value is 2～7.
7. method according to claim 6 is characterized in that, described flocculation reaction pH value is 7.
8. method according to claim 1 is characterized in that, the temperature of high temperature and high speed steam is 500-600 ℃ in the described drying and other treatment step.
9. method according to claim 1 is characterized in that, it further comprises the steps, throws in basic agent and fix and remove the sulfur-containing foul material in oily sludge.
10. method according to claim 9 is characterized in that described basic agent includes but not limited to NaOH, Na
2CO
3, NaHCO
3, Ca (OH)
2, CaO, Ca (HCO
3)
2Or its mixture.
11. method according to claim 10 is characterized in that, described basic agent addition is that mud per ton is thrown in 1～8 kilogram.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007101454603A CN100548911C (en) | 2007-09-13 | 2007-09-13 | A kind of process for treating oil-containing sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007101454603A CN100548911C (en) | 2007-09-13 | 2007-09-13 | A kind of process for treating oil-containing sludge |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101148310A CN101148310A (en) | 2008-03-26 |
| CN100548911C true CN100548911C (en) | 2009-10-14 |
Family
ID=39249024
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007101454603A Expired - Fee Related CN100548911C (en) | 2007-09-13 | 2007-09-13 | A kind of process for treating oil-containing sludge |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100548911C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103304112A (en) * | 2012-03-13 | 2013-09-18 | 侯向明 | Treatment technology and complete set of equipment for clean production of oil sludge |
Families Citing this family (37)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102167487A (en) * | 2010-02-26 | 2011-08-31 | 李红伟 | Method and equipment for drying and purifying urban and industrial sludge |
| CN101935140B (en) * | 2010-07-23 | 2012-08-29 | 无锡市通用机械厂有限公司 | Dehydration treatment method for tail water sludge of water-work and special apparatus thereof |
| CN101967033A (en) * | 2010-08-23 | 2011-02-09 | 北京纬纶华业环保科技股份有限公司 | Decrement, resource protection and innocent treatment method for tank bottom oil sludge |
| CN103011704B (en) * | 2012-12-10 | 2014-07-23 | 傅绍斌 | Method for preparing building brick from oil field oily sludge |
| CN104016558A (en) * | 2013-03-01 | 2014-09-03 | 上海科锐驰化工装备技术有限公司 | Method and device for drying sludge |
| CN103224312A (en) * | 2013-05-08 | 2013-07-31 | 上海市离心机械研究所有限公司 | Drilling sludge drying treatment process and special dewatering and drying system |
| CN104699137A (en) * | 2013-12-10 | 2015-06-10 | 北京航天中伟科技工程自动化有限公司 | Temperature control system and temperature control method for high-speed treatment system for steam with oily sludge |
| CN104250573B (en) * | 2014-09-19 | 2017-05-03 | 沈阳建筑大学 | Fuel and preparation method thereof |
| CN104402178A (en) * | 2014-11-25 | 2015-03-11 | 杰瑞能源服务有限公司 | Feeding device and system for treating oilfield waste |
| CN104860507B (en) * | 2015-06-10 | 2016-11-16 | 湖南首创投资有限责任公司 | A kind of sludge dewatering drying forming system |
| CN105000769A (en) * | 2015-08-14 | 2015-10-28 | 武汉东海石化重型装备有限公司 | Disposal system device and disposal method for oily sludge produced during smelting |
| CN105819660B (en) * | 2015-09-22 | 2019-09-03 | 北京航天试验技术研究所 | A kind of oily sludge separation equipment |
| CN105169757A (en) * | 2015-09-23 | 2015-12-23 | 邓永辉 | Waste dehydrating system |
| CN105149326B (en) * | 2015-10-15 | 2017-09-01 | 宁波金田铜业(集团)股份有限公司 | A kind of pollution-free apparatus for continuous treatment and its processing method of oil-containing copper scale |
| CN105278330A (en) * | 2015-11-06 | 2016-01-27 | 哈尔滨商业大学 | Oil sewage treatment system and treatment method based on WebAccess |
| CN105524643A (en) * | 2016-01-21 | 2016-04-27 | 辽宁石油化工大学 | Device for extracting petroleum from oily sludge |
| CN105693061A (en) * | 2016-01-22 | 2016-06-22 | 中国石油化工股份有限公司荆门分公司 | Oily sludge harmless treatment method for petrochemical wastewater treatment station |
| CN105668961B (en) * | 2016-03-09 | 2019-04-09 | 北京天灏柯润环境科技有限公司 | Sludge treatment equipment and method |
| CN106348553B (en) * | 2016-11-01 | 2019-07-23 | 天津莱特化工有限公司 | A kind of set of three mud recovery processing technique method |
| CN107129127B (en) * | 2017-06-05 | 2020-10-30 | 浙江水利水电学院 | Sludge concentration dehydration treatment method |
| CN107500501A (en) * | 2017-07-13 | 2017-12-22 | 无锡雪浪康威环保科技有限公司 | A kind of oil plant oily sludge disposal system and method |
| CN107188342A (en) * | 2017-07-25 | 2017-09-22 | 云南大地绿坤环保科技有限公司 | A kind of method of petrochemical industry greasy filth water mixed liquid quick separating |
| CN107814474B (en) * | 2017-09-12 | 2020-06-30 | 浙江山海建设有限公司 | River sludge treatment method |
| CN110104936A (en) * | 2018-01-30 | 2019-08-09 | 辽宁德智环保技术有限公司 | The method of nano polyaluminium chloride processing fermented sludge |
| CN109022079B (en) * | 2018-08-31 | 2021-01-05 | 武汉天源环保股份有限公司 | Method for preparing formed fuel by using sludge and domestic garbage of town sewage plant |
| CN109970308A (en) * | 2019-04-15 | 2019-07-05 | 厦门鹭昆机电设备有限公司 | A kind of centrifugal dehydration desiccation integral machine |
| CN110104926A (en) * | 2019-06-18 | 2019-08-09 | 中国神华煤制油化工有限公司 | A kind of DCL/Direct coal liquefaction sludge treatment equipment and method |
| CN110330198A (en) * | 2019-07-09 | 2019-10-15 | 北京和荣工程技术有限公司 | A kind of oil-sludge treatment method and system |
| CN111074085A (en) * | 2019-12-31 | 2020-04-28 | 中核内蒙古矿业有限公司 | Method and device for recycling three-phase flocculate generated by uranium extraction process |
| CN111924933B (en) * | 2020-07-09 | 2022-11-22 | 腾泽科技(无锡)有限公司 | Device for water body ecological restoration and using method thereof |
| CN111875227A (en) * | 2020-08-05 | 2020-11-03 | 江苏联兴成套设备制造有限公司 | Method for promoting oil removal in oily sludge |
| CN112374594A (en) * | 2020-11-10 | 2021-02-19 | 菏泽华意化工有限公司 | Preparation method of flocculant for treating wastewater containing cyanuric acid |
| CN112919772B (en) * | 2021-02-01 | 2022-10-21 | 武汉中科固废资源产业技术研究院有限公司 | Sludge thermal modification drying system |
| CN113698069B (en) * | 2021-10-29 | 2022-01-28 | 国能龙源环保有限公司 | Blending combustion system and blending combustion method for cooperatively treating oily sludge in coal-fired power plant |
| CN114315086B (en) * | 2022-03-14 | 2022-06-07 | 湖南中拓环境工程有限公司 | Efficient sludge drying system for sewage treatment |
| CN115583780A (en) * | 2022-10-13 | 2023-01-10 | 山东京阳科技股份有限公司 | Oily sludge treatment method |
| CN115572038A (en) * | 2022-10-26 | 2023-01-06 | 唐山睿泽尔科技有限公司 | Cold rolling oil sludge treatment system of iron and steel plant |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1992008770A1 (en) * | 1990-11-13 | 1992-05-29 | Heuer Steven R | Process for recovery of oil from waste oil sludges |
| CN1178777A (en) * | 1997-10-16 | 1998-04-15 | 河南石油勘探局炼油厂 | Process for treating oil containing sludge |
| CN2823536Y (en) * | 2005-06-30 | 2006-10-04 | 中国石油化工股份有限公司 | Steam injection heating type well head sand remover |
| US20060225925A1 (en) * | 2005-04-11 | 2006-10-12 | M-I Llc | Apparatus and method for recovering oil-based drilling mud |
-
2007
- 2007-09-13 CN CNB2007101454603A patent/CN100548911C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1992008770A1 (en) * | 1990-11-13 | 1992-05-29 | Heuer Steven R | Process for recovery of oil from waste oil sludges |
| CN1178777A (en) * | 1997-10-16 | 1998-04-15 | 河南石油勘探局炼油厂 | Process for treating oil containing sludge |
| US20060225925A1 (en) * | 2005-04-11 | 2006-10-12 | M-I Llc | Apparatus and method for recovering oil-based drilling mud |
| CN2823536Y (en) * | 2005-06-30 | 2006-10-04 | 中国石油化工股份有限公司 | Steam injection heating type well head sand remover |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103304112A (en) * | 2012-03-13 | 2013-09-18 | 侯向明 | Treatment technology and complete set of equipment for clean production of oil sludge |
| CN103304112B (en) * | 2012-03-13 | 2015-04-08 | 侯向明 | Treatment technology and complete set of equipment for clean production of oil sludge |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101148310A (en) | 2008-03-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100548911C (en) | A kind of process for treating oil-containing sludge | |
| CN108947154B (en) | A kind of intelligence oil sludge processing unit and treatment process | |
| CN101307244B (en) | Oil-making method of double-bed interactive and circling type for pyrolyzing sludge | |
| CN102503055B (en) | Treatment method and treatment apparatus of oily sludge | |
| CN106746419A (en) | A kind of oily sludge industrially scalable pyrolysis treatment systems and method | |
| US4013516A (en) | Apparatus and process for the pyrolysis of waste solids concentrates | |
| CN104748130B (en) | Oil-bearing solid waste resource utilization device and method | |
| CN101239770A (en) | Dirty oil mud separating method and device | |
| CN104211274A (en) | Sludge reduction and recycling treatment device and sludge treatment method | |
| WO2008128465A1 (en) | System and progress for treating wet sludge by drying and incinerating | |
| CN102079615A (en) | Method for harmlessly recycling sludge | |
| WO2019050431A1 (en) | Method for utilizing solid carbon-containing waste by pyrolysis and waste processing complex for implementing same | |
| US3859174A (en) | Recovery of potable water from sanitary waste using solid wastes and refuse as a heat source | |
| CN109455899A (en) | A kind of oily sludge disposal system and its disposing technique | |
| CN107500501A (en) | A kind of oil plant oily sludge disposal system and method | |
| CN112724993A (en) | System and method for oil-containing sludge cracking | |
| CN103420555A (en) | Oil sludge treating system and method | |
| CN103693823A (en) | Harmless treatment method of oil-containing sludge | |
| CN109575961A (en) | A kind of continous way industrial organic waste decomposes carbonizing plant and its method | |
| CN201190133Y (en) | Oil-bearing sludge separator | |
| CN101121571B (en) | Method for treating well drilling waste liquid by diesel engine tail gas | |
| CN108101572A (en) | The method that high viscosity tank bottom oily sludge coupling coal chemical industry solid waste prepares light ceramic | |
| CN108624347A (en) | The synchronous recycling of oil product and purification method in a kind of oily sludge | |
| CN202279767U (en) | Oily sludge treatment equipment | |
| CN203360242U (en) | Oil sludge treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20091014 Termination date: 20150913 |
|
| EXPY | Termination of patent right or utility model |