CN104261592A - Fracturing flow-back fluid treatment system and treatment technology - Google Patents
Fracturing flow-back fluid treatment system and treatment technology Download PDFInfo
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- CN104261592A CN104261592A CN201410529124.9A CN201410529124A CN104261592A CN 104261592 A CN104261592 A CN 104261592A CN 201410529124 A CN201410529124 A CN 201410529124A CN 104261592 A CN104261592 A CN 104261592A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/888—Tungsten
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/14—Phosphorus; Compounds thereof
- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
Abstract
The invention discloses a fracturing flow-back fluid treatment system and a treatment technology and aims to solve the problems that the existing fracturing flow-back fluid treatment technology pollutes the environment, waste the resources and is high in fracturing construction cost. The fracturing flow-back fluid treatment system comprises a flow-back fluid reaction device, a first screw pump, a press filter, a filtrate fine filter, a third screw pump, a filter membrane assembly and a water storage tank, which are sequentially connected, and a solid phase collecting tank connected with the press filter. The fracturing flow-back fluid treatment system is reasonable in structure, simple in process and convenient to operate, and can greatly reduce environment pollution, improve the recycling utilization value of fracturing flow-back fluid and reduce treatment cost and later fracturing construction cost, thereby having high application value.
Description
Technical field
The present invention relates to a kind of fracturing outlet liquid treatment system and treatment process thereof.
Background technology
Along with of the fracturing fluid development, of the fracturing fluid Low Damage, low cost require also more and more outstanding.Simultaneously, along with the application of big-frac treatment increase oil-gas mining measure in oil-gas field is more and more extensive, especially the exploitation of shale gas, coal-seam gas, fracturing liquid by original tens, hundreds of side is increased to current upper all places, fast-developing to multiple pressure break by substance pressure break, therefore returning the waste liquid amount ejected after pressure break also significantly increases.
Post-fracturing waste liquid consists predominantly of slippery water stoste and returns discharge opeing, and polymkeric substance, salt, suspended substance, heavy metal ion and other additive.Arrange if fracturing outlet liquid is directly outer without process, will to surrounding environment, especially farm crop and surface drainage system pollute, and processing costs is simultaneously higher.Therefore, discharge opeing will be returned and recycle and better can not only solve environmental problem, and the area such as, desert undeveloped to environment sensitive region and underground water, surface drainage system and offshore oil and gas exploitation have great using value.
But, mostly adopt the mode of purification of waste water to process to fracturing outlet liquid both at home and abroad at present, generally do not recycle, and not only easily cause environmental pollution, processing costs higher like this, and waste resource.If can well fracturing outlet liquid be recycled, then will reduce environmental pollution to a great extent, and improve the value of fracturing outlet liquid, the construction cost of later stage pressure break can also be saved simultaneously.
In sum, design a set of suitable technical process, system and new medicament and fracturing outlet liquid is processed, realize recycling, avoid environmental pollution, improve the value returning discharge opeing, and reduce the cost of pressing crack construction, just become one of content of those skilled in the art's primary study.
Summary of the invention
The object of the present invention is to provide a kind of fracturing outlet liquid treatment system and treatment process thereof, mainly solve existing fracturing outlet liquid treatment process and there is contaminate environment, waste resource and the high problem of pressing crack construction cost.
To achieve these goals, the technical solution used in the present invention is as follows:
A kind of fracturing outlet liquid treatment system, comprise connect successively return discharge opeing reaction unit, the first spiral pump, pressure filter, filtrate fine filtering device, three-screw pump, filter membrane component and water tank, and the solid phase holding tank be connected with pressure filter.
Further, described filter membrane component returns to be connected in and returns discharge opeing reaction unit.
Specifically, described in return discharge opeing reaction unit and comprise submersible sewage pump, the retort be connected with this submersible sewage pump, be arranged on the stirrer in this retort, grug feeding jar tank connected with this reaction, and respectively with stirrer and the tank connected housing of dosing; Described retort is connected with the first spiral pump and filter membrane component respectively.
Specifically, described filtrate fine filtering device comprises the filtrate collection case be connected with pressure filter, and the smart filter tower be connected with this filtrate collection case by the second spiral pump; Described smart filter tower is connected with three-screw pump.
Again further, described retort is two, and described submersible sewage pump and the first spiral pump are connected with two retort all simultaneously.
Further, described submersible sewage pump, retort, grug feeding jar, housing, the first spiral pump, pressure filter, solid phase holding tank, filtrate collection case, the second spiral pump, smart filter tower, three-screw pump, filter membrane component and water tank are sledge-borne type structure.
Based on said structure basis, present invention also offers the treatment process of this fracturing outlet liquid, comprise the following steps:
(1) utilize submersible sewage pump will return discharge opeing to continue to be pumped in retort from returning discharge opeing retention basin, until the water level in retort reaches its working water level;
(2) start stirrer, and respectively acid PH conditioning agent and oxygenant are joined uniform stirring in retort, fully react until return discharge opeing and acid PH conditioning agent and oxygenant, the pH value of reacted solution is 3.0 ~ 6.0;
(3) by grug feeding jar flocculation agent joined in retort and continue uniform stirring, until the impurity returned in discharge opeing is separated out with solid precipitation form;
(4) utilize the first spiral pump will return discharge opeing to be pumped in pressure filter and to carry out mud solid-liquid separation;
(5) liquid of separation is input in filtrate collection case and collects by pressure filter, and filtrate to be pumped in smart filter tower by the second spiral pump and to carry out secondary filtration;
(6) by three-screw pump the filtrate after secondary filtration is pumped in filter membrane component and carries out advanced treatment, make filtrate reach emission standard, and collected in water tank.
Further, described oxygenant is iron sila polyacid catalytic oxidant, and its preparation process is as follows:
A () utilizes 350 ~ 400g deionized water by the acid hydrolysis of 90 ~ 95g phosphorus crane, obtain hydrating solution;
B () adds 16 ~ 17g ferrous sulfate in hydrating solution, and under 50 ~ 55 DEG C of constant temperatures, drip sodium bicarbonate and water glass saturated solution respectively, until the pH value of solution is 3 ~ 3.5;
(c) cold and dressed with sauce 30 ~ 40min, and solution is filtered;
D filtrate is evaporated to half thick shape by () under 65 ~ 75 DEG C of conditions, and leave standstill, until there is colourless acicular crystal to separate out;
E filtrate is filtered by (), then dry, standing, until there is bulk crystals to separate out;
F () repeating step (e) once, the crystal obtained is oxygenant.
Again further, described acid PH conditioning agent is organic acid, and described flocculation agent is ferric sulfate.
Further, in described step (6), if filtrate does not reach emission standard, then filtrate is returned in retort, and iterative cycles step (2) ~ (6), until filtrate reaches emission standard.
Compared with prior art, the present invention has following beneficial effect:
(1) the present invention is reasonable in design, and flow process is succinct, easy to operate.
(2) the present invention is by the combination of equipment and technology, adopt the mode of preoxidation, flocculation, press filtration, essence filter, film process, purifying treatment has been carried out to fracturing outlet liquid, effectively can not only remove the impurity in fracturing outlet liquid and additive, and significantly reducing the content of its COD, fracturing outlet liquid is possessed, and very high recycling is worth.Meanwhile, the present invention can be directly up to standard by liquid waste disposal at the scene, thus not only saved the cost of amount transport and process, evades waste liquid contingent risk of leakage in transit, and fundamentally solve the problem of contaminate environment.
(3) the present invention is with the acid of phosphorus crane, deionized water, ferrous sulfate, sodium bicarbonate, water glass saturated solution is as raw material, and combine a kind of new technique to prepare oxygenant, this kind of oxygenant is compared with existing single-oxidizer, there is catalytic activity high, the advantage that redox ability is strong, and it also has the characteristic of strong acid, very easily be dissolved in organic solvent (such as fracturing outlet liquid), therefore, under suitable PH environment, oxygenant prepared by the present invention can react with fracturing outlet liquid fully, realize the preoxidation returning discharge opeing, thus provide good reaction environment and condition for the follow-up flocculation returning discharge opeing, the impurity returned in discharge opeing is separated out with the form of solid precipitation completely.
(4) Parallel Design of the present invention two retort, so that be used alternatingly, thus realize the continuous process to fracturing outlet liquid.
(5) the present invention counts absolutely greatly the structure that equipment all adopts sledge-borne type, can with any transition of drilling team, maneuvering ability is larger, can need to combine treatment facility according to process, thus meet and process returning discharge opeing and recycle at the scene, thus, not only can avoid causing environmental pollution, reduce processing costs, and the value of the fracturing outlet liquid that economizes on resources, improves, and effectively save the construction cost of later stage pressure break.
(6) the present invention studies and design by being engaged in oil-gas mining field work senior engineer officer for many years, and verified by test of many times, thus achieve the combination of theory and practice well, achieve great innovation, the present invention has very strong practicality and versatility, is suitable for large-scale promotion application.
Accompanying drawing explanation
Fig. 1 is device structure schematic diagram of the present invention.
Fig. 2 is process flow diagram of the present invention.
Wherein, the component name that Reference numeral is corresponding is called:
1-submersible sewage pump, 2-retort, 3-stirrer, 4-grug feeding jar, 5-housing, 6-first spiral pump, 7-pressure filter, 8-solid phase holding tank, 9-filtrate collection case, 10-second spiral pump, 11-essence filter tower, 12-three-screw pump, 13-filter membrane component, 14-water tank.
Embodiment
Below in conjunction with drawings and Examples, the invention will be further described, and embodiments of the present invention include but not limited to the following example.
Embodiment
The invention provides a kind for the treatment of system of fracturing outlet liquid, as shown in Figure 1, this treatment system comprises and returns discharge opeing reaction unit, the first spiral pump 6, pressure filter 7, solid phase holding tank 8, filtrate fine filtering device, three-screw pump 12, filter membrane component 13 and water tank 14.The described discharge opeing reaction unit that returns is separated out with the form of solid precipitation for the impurity that will return in discharge opeing, it comprises submersible sewage pump 1, the retort 2 be connected with this submersible sewage pump 1, be arranged on the stirrer 3 in this retort 2, the grug feeding jar 4 be connected with this retort 2, and the housing 5 be connected with stirrer 3 and grug feeding jar 4 respectively; Described retort 2 is connected with the first spiral pump 6.
Described pressure filter 7 is for carrying out mud solid-liquid separation by separating out the discharge opeing of returning after solid impurity, and as preferably, in the present embodiment, this pressure filter 7 is plate-and-frame filter press.Solid phase holding tank 8 is then connected with pressure filter 7, for collecting the solid slag after returning discharge opeing press filtration.
Described filtrate fine filtering device is used for the liquid of separation to carry out secondary filtration, to remove the minute impurities in filtrate, this filtrate fine filtering device comprises the filtrate collection case 9 be connected with pressure filter 7, and the smart filter tower 11 be connected with this filtrate collection case 9 by the second spiral pump 10; Described smart filter tower 11 is connected with three-screw pump 12.
Described three-screw pump 12, filter membrane component 13 and water tank 14 connect successively, and filter membrane component 13, for filtrate is carried out advanced treatment, makes it reach emission standard, is then collected in water tank 14, finally recycles according to actual needs.
Utilize aforesaid device structure, below the flow process of process fracturing outlet liquid of the present invention is described in detail.
As shown in Figure 2, first, utilize submersible sewage pump 1 will return in discharge opeing retention basin to return discharge opeing and continue to be pumped in retort 2.Then, control stirrer 3 by housing 5 to open, then acid PH conditioning agent and oxygenant are joined in retort 2 and be uniformly mixed, make to return discharge opeing fully to react, and reacted pH value is 3.0 ~ 6.0, and then control grug feeding jar 4 flocculation agent is joined in retort 2 continue stir, make to return the impurity in discharge opeing and separate out with the form of solid precipitation.Retort 2 in the present embodiment and grug feeding jar 4 all arrange two, thus adopt the mode replaced in parallel, realize the continuous process returning discharge opeing.Acid PH conditioning agent, oxygenant and flocculation agent that the present embodiment is used then are respectively organic acid, iron sila polyacid catalytic oxidant and ferric sulfate, wherein, the present embodiment is using the acid of phosphorus crane, deionized water, ferrous sulfate, sodium bicarbonate, water glass saturated solution as raw material, and combine a kind of new preparation technology and carry out obtained iron sila polyacid catalytic oxidant, its preparation process is as follows:
(1) utilize 350 ~ 400g deionized water by the acid hydrolysis of 90 ~ 95g phosphorus crane, obtain hydrating solution;
(2) in hydrating solution, add 16 ~ 17g ferrous sulfate, and under 50 ~ 55 DEG C of constant temperatures, drip sodium bicarbonate and water glass saturated solution respectively, until the pH value of solution is 3 ~ 3.5;
(3) cold and dressed with sauce 30 ~ 40min, and solution is filtered;
(4) under 65 ~ 75 DEG C of conditions, filtrate is evaporated to half thick shape, and leaves standstill, until there is colourless acicular crystal (Na
2sO
4.nH
2o) separate out;
(5) filtrate is filtered, then dry, standing, until there is bulk crystals to separate out;
(6) repeating step (5) once, the crystal (Na obtained
5[SiW
11o
39fe]) be oxygenant.
Return discharge opeing to separate out after solid precipitation, open the valve of retort 2, then returning discharge opeing by the first spiral pump 6 and be pumped in pressure filter 7 and carry out mud solid-liquid separation, and realizing the preliminary treatment to returning discharge opeing.After separation, collect Gu slag enters into solid phase holding tank 8, the liquid containing a small amount of minute impurities then enters into filtrate collection case 9 and collects.
Then, utilize the second spiral pump 10 to be pumped into by liquid in smart filter tower 11 and carry out secondary filtration, the minute impurities in removing liquid, obtain not containing the filtrate of solid impurity.Finally recycle three-screw pump 12 filtrate is pumped in filter membrane component 13 carries out advanced treatment, make filtrate reach emission standard, then collect in water tank 14.In said process, after filter membrane component 13 processes filtrate, if do not reach emission standard, then can filtrate be turned back to retort 2 from filter membrane component 13, and then the above-mentioned treating processes of recirculation, until after filtrate reaches emission standard, then collected in water tank 14.
Equipment of the present invention, such as submersible sewage pump 1, retort 2, grug feeding jar 4, housing 5, first spiral pump 6, pressure filter 7, solid phase holding tank 8, filtrate collection case 9, second spiral pump 10, essence filter tower 11, three-screw pump 12, filter membrane component 13 and water tank 14, be all that equipment (is such as fixed on a chassis of being made up of angle steel or joist steel by sledge-borne type structure, then crowbar or weight handling equipment is used to be moved with in place), a whole set for the treatment of system so can be facilitated with any transition of drilling team, its maneuvering ability is very good, and can need to combine equipment according to process, meet on-the-spot to process and the recycling of returning discharge opeing.
For embodying the present invention to the treatment effect returning discharge opeing, the fracturing liquid returning discharge opeing preparation after verifying process of the present invention with several test case below, whether the performance of its each side can meet the requirement of pressing crack construction, thus embodies the recycling value returning discharge opeing further.
Case 1: the of the fracturing fluid gel-forming property test of secondary preparation
Utilize the discharge opeing of returning after process to be mixed with fracturing liquid, then measure 100ml fracturing liquid base fluid with graduated cylinder, and pour in glass beaker.Under glass stick whipped state, the linking agent accurately pipetting 0.4mL with transfer pipet joins in base fluid, and then by manual time-keeping, record base fluid plays plastic (can hang) required time.After Gel Formation, hang with glass stick, by range estimation and transparency, toughness, elasticity, the intensity of micro-judgment frozen glue.Table 1 forms the performance test results after frozen glue for utilizing several fracturing liquids returning discharge opeing preparation:
Table 1
As can be seen from Table 1, utilize the fracturing liquid returning discharge opeing preparation after process of the present invention, gelation time is very fast, and can reach 64s, thus cross-linking effect is all good.And the frozen glue transparency formed, hanging property are good, meet the requirement returning discharge opeing recycling completely.
Case 2: the of the fracturing fluid heat resistance test of secondary preparation
After treatment return in discharge opeing, add the guanidine glue of 35% and the cross-linked rubber of 0.4% respectively, other treatment agents then add according to on-the-spot formula system, then by change temperature carry out the impact of probe temperature on gelatin viscosity, test result is as shown in table 2:
| Gelling temperature/DEG C | 30 | 60 | 70 | 75 | 80 | 90 |
| Apparent viscosity (mPas, 170s -1） | 690 | 380 | 205 | 190 | 145 | 65 |
Table 2
As can be seen from Table 2, along with the increase of temperature, the viscosity of glue is on a declining curve, and when temperature is elevated to 80 DEG C, gelatin viscosity is 145 mPas, and this viscosity can meet site operation and take sand performance requriements.
Case 3: the of the fracturing fluid residue content test of secondary preparation
Residue is water-insoluble residual in fracturing liquid rubber-breaking liquid.The existence of residue plugs sand packed fracture, reduces the flow conductivity in reservoir infiltration filter and crack.The testing method of residue content: 50mL breaking glue solution is moved in the 50mL centrifuge tube of constant weight, at 3000rmin
-1rotating speed under centrifugal 30min, then supernatant liquid is toppled over, and be again poured in centrifuge tube after washing brokenly glue container with water and continue centrifugal 30min, remove supernatant liquid again, centrifuge tube is placed in baking oven dry to constant weight, finally namely obtains of the fracturing fluid residue content with mass of residue divided by fracturing liquid consumption.
Table 3 for returning discharge opeing preparing fracturing fluid after adopting process, in identical formula situation, contrast clear water preparing fracturing fluid with return discharge opeing configure fracturing liquid rubber-breaking after residue situation:
| Preparing fracturing fluid liquid phase | Clear water | Soviet Union 59-7-51 | Public 26-2 | High mountain 10/-44-H1 |
| Level of residue/g after broken glue | 0.1984 | 0.2077 | 0.1985 | 0.2103 |
Table 3
As can be seen from Table 3, adopt the fracturing liquid returning discharge opeing preparation after process, after broken glue, its level of residue is only slightly high than the residue content of clear water preparation, and this is for no other reason than that return in discharge opeing inherently containing some impurity, so, adopt process after return discharge opeing preparing fracturing fluid, it can meet the requirement of pressing crack construction completely.
Case 4: the of the fracturing fluid outstanding sand aptitude tests of secondary preparation
Of the fracturing fluid outstanding grittiness is the key ensureing pressing crack construction, and the evaluation of fracturing liquid being hanged to grittiness energy is divided into dynamically outstanding sand and static state to hang sand.Generally, the outstanding sand Performance Evaluating Indexes of guanidine colloid system is of the fracturing fluid viscosity, and the outstanding sand Performance Evaluating Indexes of clean fracturing fluid is of the fracturing fluid viscoelasticity.Static outstanding sand experiment is easy to operate, laboratory experiment is that the fracturing liquid prepared is put into 50mL graduated cylinder, graduated cylinder is made to be placed in water-bath or the oil bath of probe temperature, put quartz sand into graduated cylinder, it is made to do free setting campaign, using the time of sedimentation divided by measuring graduated cylinder height as sand setting speed, with the evaluation of sand setting speed as outstanding grittiness energy.At present in China, dynamically outstanding sand device is by a set of model of Xi'an Communications University's development research, then High-speed Photography Technology is applied, the settlement law of fracturing liquid horizontal flow process particle is studied in square crack, for being familiar with the settlement law of fracturing process particle in formation fracture and the of the fracturing fluid prop-carrying capacity of assessment, provide more reliable foundation.
Table 4 for returning discharge opeing preparing fracturing fluid after adopting process, in identical formula situation, contrast clear water preparing fracturing fluid with return discharge opeing and configure of the fracturing fluid suspended prop aptitude tests, wherein, propping agent adopts quartz sand:
| Preparing fracturing fluid liquid phase | Clear water | Soviet Union 59-7-51 well returns discharge opeing | Public 26-2 well returns discharge opeing | High mountain 10/-44-H1 well returns discharge opeing |
| Outstanding sand time/min | 25 | 25 | 23 | 21 |
Table 4
As can be seen from Table 4, adopt process after return discharge opeing preparing fracturing fluid, the fracturing liquid suspended prop ability that the ability of its suspended prop and clear water are prepared is more or less the same, and therefore meets the requirement of pressing crack construction completely.
Case 5: the of the fracturing fluid anti-dilative test of secondary preparation
Adopt the of the fracturing fluid anti-dilative of centrifugal determination.Of the fracturing fluid anti-dilative is evaluated by measuring the volumetric expansion increment of bentonite in powder in clay stabilizer solution and water.Its operating process is: take 0.50g wilkinite, loads in 10mL centrifuge tube, adds the breaking glue solution of the different dosage clay stabilizer of 10mL, fully shake up, at 70 DEG C, leave standstill 2h, load in whizzer, centrifugation 15min under rotating speed is 1500r/min, read bentonite inflated after volume V
1.Replace stabilizing solution with 10mL water and kerosene respectively, measure the expanding volume V of wilkinite in water and in kerosene
2, V
0, anti-dilative calculation formula is as follows.
In formula: B
1---anti-dilative, %;
V
1---bentonite in powder in clay stabilizer solution expanding volume, mL;
V
2---bentonite in powder is expanding volume in water, mL;
V
0---bentonite in powder is expanding volume in kerosene, mL.
According to above-mentioned formula, calculate several by utilizing the of the fracturing fluid anti-dilative returning discharge opeing preparation after processing, result is as shown in table 5:
Table 5
As can be seen from Table 5, adopt process after return discharge opeing preparing fracturing fluid, its anti-dilative is higher, can reach more than 92%, thus effectively can avoid the problem causing due to hydration and expansion of clay zone permeability to reduce in the earth formation, thus improve stimulation work effect.
The present invention achieves the process to fracturing outlet liquid well, make it can repeatedly recycling, not only avoid fracturing outlet liquid because dealing with improperly the problem to environment, and significantly reduce the cost of process and the construction cost of later stage pressure break, therefore, the present invention is compared to existing technology, progressive fairly obvious, and it has outstanding substantive distinguishing features and significant progress.
Above-described embodiment is only the preferred embodiments of the present invention; be not construed as limiting the scope of the present invention; in every case principle of design of the present invention being adopted, and the change carried out non-creativeness work on this basis and make, all should belong within protection scope of the present invention.
Claims (10)
1. a fracturing outlet liquid treatment system, it is characterized in that, comprise connect successively return discharge opeing reaction unit, the first spiral pump (6), pressure filter (7), filtrate fine filtering device, three-screw pump (12), filter membrane component (13) and water tank (14), and the solid phase holding tank (8) be connected with pressure filter (7).
2. a kind of fracturing outlet liquid treatment system according to claim 1, is characterized in that, described filter membrane component (13) returns to be connected in and returns discharge opeing reaction unit.
3. a kind of fracturing outlet liquid treatment system according to claim 2, it is characterized in that, the described discharge opeing reaction unit that returns comprises submersible sewage pump (1), the retort (2) be connected with this submersible sewage pump (1), be arranged on the stirrer (3) in this retort (2), the grug feeding jar (4) be connected with this retort (2), and the housing (5) be connected with stirrer (3) and grug feeding jar (4) respectively; Described retort (2) is connected with the first spiral pump (6) and filter membrane component (13) respectively.
4. a kind of fracturing outlet liquid treatment system according to claim 3, it is characterized in that, described filtrate fine filtering device comprises the filtrate collection case (9) be connected with pressure filter (7), and the smart filter tower (11) be connected with this filtrate collection case (9) by the second spiral pump (10); Described smart filter tower (11) is connected with three-screw pump (12).
5. a kind of fracturing outlet liquid treatment system according to claim 4, is characterized in that, described retort (2) is two, and described submersible sewage pump (1) and the first spiral pump (6) are connected with two retort (2) all simultaneously.
6. a kind of fracturing outlet liquid treatment system according to claim 4 or 5, it is characterized in that, described submersible sewage pump (1), retort (2), grug feeding jar (4), housing (5), the first spiral pump (6), pressure filter (7), solid phase holding tank (8), filtrate collection case (9), the second spiral pump (10), smart filter tower (11), three-screw pump (12), filter membrane component (13) and water tank (14) are sledge-borne type structure.
7. a fracturing outlet liquid treatment process, is characterized in that, comprises the following steps:
(1) utilize submersible sewage pump will return discharge opeing to continue to be pumped in retort from returning discharge opeing retention basin, until the water level in retort reaches its working water level;
(2) start stirrer, and respectively acid PH conditioning agent and oxygenant are joined uniform stirring in retort, fully react until return discharge opeing and acid PH conditioning agent and oxygenant, the pH value of reacted solution is 3.0 ~ 6.0;
(3) by grug feeding jar flocculation agent joined in retort and continue uniform stirring, until the impurity returned in discharge opeing is separated out with solid precipitation form;
(4) utilize the first spiral pump will return discharge opeing to be pumped in pressure filter and to carry out mud solid-liquid separation;
(5) liquid of separation is input in filtrate collection case and collects by pressure filter, and filtrate to be pumped in smart filter tower by the second spiral pump and to carry out secondary filtration;
(6) by three-screw pump the filtrate after secondary filtration is pumped in filter membrane component and carries out advanced treatment, make filtrate reach emission standard, and collected in water tank.
8. a kind of fracturing outlet liquid treatment process according to claim 7, is characterized in that, described oxygenant is iron sila polyacid catalytic oxidant, and its preparation process is as follows:
A () utilizes 350 ~ 400g deionized water by the acid hydrolysis of 90 ~ 95g phosphorus crane, obtain hydrating solution;
B () adds 16 ~ 17g ferrous sulfate in hydrating solution, and under 50 ~ 55 DEG C of constant temperatures, drip sodium bicarbonate and water glass saturated solution respectively, until the pH value of solution is 3 ~ 3.5;
(c) cold and dressed with sauce 30 ~ 40min, and solution is filtered;
D filtrate is evaporated to half thick shape by () under 65 ~ 75 DEG C of conditions, and leave standstill, until there is colourless acicular crystal to separate out;
E filtrate is filtered by (), then dry, standing, until there is bulk crystals to separate out;
F () repeating step (e) once, the crystal obtained is oxygenant.
9. a kind of fracturing outlet liquid treatment process according to claim 8, is characterized in that, described acid PH conditioning agent is organic acid, and described flocculation agent is ferric sulfate.
10. a kind of fracturing outlet liquid treatment process according to claim 9, is characterized in that, in described step (6), if filtrate does not reach emission standard, then filtrate is returned in retort, and iterative cycles step (2) ~ (6), until filtrate reaches emission standard.
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