A production device and method of a cementing oil well cement retarder

Abstract

This invention relates to the field of reactor technology, specifically disclosing a production apparatus and method for a cement retarder for well cementing. The production apparatus includes: a reactor unit; a circumferential mixing unit; a nitrogen distribution unit; a tiered turbulence unit; and an initiator injection unit. The nitrogen distribution unit rotates with a rotating shaft, causing nitrogen to spiral upwards from the bottom of the reactor and break into microbubbles, forming a uniform anaerobic flow field. This avoids oxygen inhibiting polymerization and ensures the uniformity of the retarder's molecular weight. The initiator injection unit rotates synchronously, ejecting the initiator to achieve high-speed shear mixing, preventing excessively high local concentrations and gel particle formation, and improving product purity and solubility stability. The tiered turbulence unit is driven by nitrogen, periodically pushing the accumulated material at the bottom upwards to the main stirring zone, eliminating dead zones at the bottom of the reactor and batch-to-batch differences, effectively improving production reproducibility and batch stability.

Description

Technical Field

[0001] This invention relates to the field of reaction vessel technology, and more specifically, to a production apparatus and method for a cement retarder for well cementing. Background Technology

[0002] Currently, cement retarders are mainly produced through a synthetic reaction process. This process generates retarders through chemical reactions and is the mainstream production method for polymer-based retarders. Its core steps are as follows: Step 1: Dissolve monomers such as 2-acrylamide-2-methylpropanesulfonic acid and maleic acid in deionized water; Step 2: Under the protection of an inert gas (such as nitrogen), add an initiator and heat, carrying out a polymerization reaction under continuous stirring; Step 3: Physically compound and stir the polymer generated from the reaction with other components such as sodium hexametaphosphate and citric acid to obtain the final product. In polymerization reactions, initiators (such as ammonium persulfate) need to be added to the system uniformly at a specific temperature to control the reaction rate. In existing reactors, the initiator feed port is usually located on one side of the top of the reactor. After the initiator solution is dripped into the liquid surface, it relies on stirring to diffuse. For high viscosity systems, the diffusion rate is extremely slow, which leads to the enrichment of the initiator in local areas, causing rapid polymerization and forming hot spots of explosive polymerization, producing insoluble gel particles, which seriously affects the filtration performance and retardation effect of the product. In addition, the polymerization reaction requires the introduction of nitrogen to remove dissolved oxygen from the system. However, the nitrogen distribution in the existing reactor cannot form a uniform bubble flow field in the entire reaction system. The residual dissolved oxygen in local areas will inhibit free radical polymerization, resulting in low monomer conversion rate, and the generation of a large number of oligomers and residual monomers, which will affect the purity and quality stability of the product. Summary of the Invention

[0003] To overcome the above-mentioned technical problems, this invention proposes a production apparatus and method for a cement retarder for oil wells.

[0004] The objective of this invention can be achieved through the following technical solutions: A production apparatus for a cementing retarder for oil wells includes: A reaction vessel unit includes a vessel body, with a first feeding pipe and a second feeding pipe respectively provided at the top of the vessel body, and a discharge port provided at the bottom of the vessel body; A circumferential mixing unit includes a drive motor fixedly installed on the top of the vessel body, a rotating shaft extending vertically into the vessel body at the output end of the drive motor, and a stirring blade installed at the lower end of the rotating shaft. A nitrogen distribution unit is installed inside a rotating shaft and rotates with the shaft. Nitrogen gas is introduced through the rotating shaft and ejected from the nitrogen distribution unit into the liquid phase. The tiered turbulence unit is located at the bottom of the vessel and is used to agitate the bottom region of the vessel to generate local turbulence and periodically push the accumulated material upward to the main stirring zone. The initiator injection unit is located inside the rotating shaft and rotates with the rotating shaft. The initiator is introduced through the rotating shaft and ejected into the liquid phase from the initiator injection unit.

[0005] As a further aspect of the present invention: the nitrogen distribution unit includes a nitrogen flow channel axially opened within a rotating shaft, an exhaust chamber communicating with the nitrogen flow channel is opened at the lower end of the rotating shaft, and a plurality of internal exhaust grooves are opened circumferentially on the outer side of the exhaust chamber; a support base is fixed at the bottom of the reactor body, the lower end of the rotating shaft is rotatably embedded in the support base, and a plurality of external exhaust grooves adapted to the internal exhaust grooves are opened circumferentially on the support base.

[0006] As a further aspect of the present invention: the hierarchical turbulence unit includes several sets of hinge seats circumferentially distributed on the support base, a turbulence baffle is rotatably mounted on the hinge seat, a flexible bladder is provided on the outside of the support base to abut against the turbulence baffle, the interior of the flexible bladder is connected to each external exhaust groove, and an annular one-way valve plate is provided at the bottom of the flexible bladder, the annular one-way valve plate is provided with several exhaust holes circumferentially.

[0007] As a further aspect of the present invention: the initiator injection unit includes an initiator flow channel axially opened within the rotating shaft, the initiator flow channel being distributed parallel to the nitrogen flow channel, and a drain port being provided at the lower end of the initiator flow channel; The top of the vessel is provided with a hollow sleeve, and the hollow sleeve is provided with a gas supply component that is connected to the nitrogen flow channel and an injection component that is connected to the initiator flow channel.

[0008] As a further aspect of the present invention: the gas supply component includes a gas supply chamber disposed in a hollow sleeve, an air inlet pipe connected to one side of the gas supply chamber, a transition chamber communicating with a nitrogen flow channel is opened in the rotating shaft, and a plurality of through holes communicating with the interior of the gas supply chamber are opened circumferentially on the outer side of the transition chamber. The injection component includes an injection cavity disposed within a hollow sleeve, an injection pipe connected to one side of the injection cavity, and an inlet on the rotating shaft that connects the initiator flow channel and the injection cavity.

[0009] As a further aspect of the present invention, it also includes an anti-agglomeration impact unit disposed above the stirring blade. The anti-agglomeration impact unit includes several slide rails circumferentially distributed on the inner wall of the vessel. A lifting plate is slidably mounted on the slide rails, and an impact mesh is disposed inside the lifting plate. A spiral sleeve is fixedly sleeved on the rotating shaft. A spiral groove is formed on the spiral sleeve, and a locking pin adapted to the spiral groove is provided on the lifting plate.

[0010] As a further aspect of the present invention: a sliding cavity is provided inside the lifting plate, and the locking pin is radially slidably embedded in the sliding cavity; a magnetic block adapted to the locking pin is provided at the lower end of the spiral groove, and an impact hole communicating with the nitrogen flow channel is provided at the upper end of the spiral groove.

[0011] As a further embodiment of the present invention: a powder feeding unit is also provided above the anti-agglomeration impact unit. The powder feeding unit includes a conical guide plate fixed to the inner wall of the reactor. An annular collecting plate is horizontally provided at the lower end of the conical guide plate. A mounting frame is fixed on the rotating shaft. A comb tooth adapted to the annular collecting plate is provided at the end of the mounting frame away from the rotating shaft.

[0012] As a further embodiment of the present invention: a discharge unit is provided at the discharge port, the discharge unit includes a discharge pipe rotatably installed in the discharge port, the upper end of the discharge pipe is provided with a plurality of inner discharge ports in the circumferential direction, and the bottom of the support base is provided with a plurality of outer discharge ports adapted to the inner discharge ports in the circumferential direction.

[0013] This invention also discloses a production method using a production apparatus for cementing oil well cement retarder, comprising the following steps: Step 1: Add 2-acrylamide-2-methylpropanesulfonic acid and maleic acid monomers to the deionized water in the reactor through the first and second feeding pipes respectively in a preset ratio; Step 2: Start the drive motor to drive the stirring blades at the lower end of the shaft to rotate continuously, thus breaking up and stirring the mixed solution; Step 3: Nitrogen gas is continuously introduced into the liquid phase through an independent channel inside the rotating shaft. The nitrogen gas enters from all directions from the bottom of the vessel and rises spirally to form a uniform bubble flow field to remove local dissolved oxygen residue. Step 4: Inject the initiator solution into the liquid phase through the independent channel inside the rotating shaft to ensure rapid and uniform mixing, and avoid local enrichment to prevent the formation of insoluble gel particles. Step 5: The liquid phase is heated and continuously stirred to carry out the polymerization reaction, generating a polymer semi-finished product; Step 6: During the nitrogen injection process, the hierarchical turbulence unit is driven to move axially and periodically, throwing the bottom accumulated material upward into the main stirring zone to prevent the deposition of high-viscosity slurry.

[0014] The beneficial effects of this invention are: The nitrogen distribution unit is located inside the rotating shaft and rotates with it. Nitrogen enters the liquid phase from the bottom of the vessel from all directions. Under the action of centrifugal force, the bubbles rise in a spiral shape and cover the entire cross-section of the vessel. At the same time, the shear force generated by the rotation breaks the large bubbles into micro bubbles, forming a uniform and stable bubble flow field. This avoids the problem of local dissolved oxygen residue, effectively improves the deoxygenation effect of the polymerization reaction, avoids the inhibition of free radical polymerization by oxygen, and ensures the uniformity of the molecular weight and structure of the retarder. The initiator injection unit rotates with the shaft, and the initiator solution is thrown out from the rotating unit through the independent channel inside the shaft, achieving high-speed shear mixing with the reaction liquid. This avoids the instantaneous high concentration of the initiator in a local area, effectively preventing insoluble gel particles generated by rapid polymerization, thereby greatly improving the purity and dissolution stability of the product and ensuring the consistent flow properties of the cementing slurry. The tiered turbulence unit is located at the bottom of the reactor and is driven in conjunction with the nitrogen injection process to generate axial periodic motion. This motion can both stir the bottom area to form local turbulence and periodically push the deposited high-viscosity polymer slurry upward to the main stirring zone, avoiding the accumulation of materials in the dead corners at the bottom of the reactor in the high-viscosity reaction system and the batch-to-batch differences in molecular weight distribution and composition caused by deposition, thus effectively improving production reproducibility and product batch stability. Attached Figure Description

[0015] The invention will now be further described with reference to the accompanying drawings.

[0016] Figure 1 This is a three-dimensional structural diagram of the present invention; Figure 2 This is a three-dimensional structural schematic diagram from another perspective of the present invention; Figure 3 This is a cross-sectional structural diagram of the present invention; Figure 4 This is a schematic diagram of the internal structure of the vessel body in this invention; Figure 5 for Figure 4 Enlarged view of point A in the middle; Figure 6 This is a cross-sectional view of the hollow sleeve in this invention; Figure 7 for Figure 6 Enlarged view at point B in the middle; Figure 8 for Figure 6 Enlarged view at point C; Figure 9 This is a schematic diagram of the anti-agglomeration impact unit in the present invention; Figure 10 for Figure 9 Enlarged view at point D; Figure 11 for Figure 9 Enlarged view at point E in the middle; Figure 12 for Figure 3 Enlarged view at point F; Figure 13 for Figure 4 Enlarged view of point G in the middle.

[0017] In the picture: 100. Reactor unit; 110. Reactor body; 120. First feed pipe; 130. Second feed pipe; 140. Discharge port; 150. Hollow sleeve; 200. Circumferential mixing unit; 210. Drive motor; 220. Rotary shaft; 230. Mixing blades; 240. Support base; 241. External exhaust vent; 242. External discharge port; 300. Nitrogen distribution unit; 310. Nitrogen flow channel; 311. Impact hole; 320. Exhaust chamber; 321. Internal exhaust groove; 330. Gas supply component; 331. Gas supply cavity; 332. Inlet pipe; 333. Transition cavity; 334. Through hole; 400, Hierarchical turbulence unit; 410, Hinge seat; 420, Turbulence baffle; 430, Flexible capsule; 440, Annular one-way valve; 441, Exhaust port; 500. Anti-agglomeration impact unit; 510. Slide rail; 520. Lifting plate; 521. Slide cavity; 522. Locking pin; 523. Magnetic block; 530. Impact mesh; 540. Spiral sleeve; 550. Spiral groove; 600. Powder feeding unit; 610. Conical guide plate; 620. Annular collecting plate; 630. Mounting frame; 640. Comb teeth; 700. Discharge unit; 710. Discharge pipe; 711. Internal discharge port; 800, Initiator injection unit; 810, Initiator flow channel; 820, Drain port; 830, Injection component; 831, Injection chamber; 832, Injection pipe; 833, Inlet port. Detailed Implementation

[0018] The subject matter described herein will now be discussed with reference to exemplary embodiments. It should be understood that these embodiments are discussed only to enable those skilled in the art to better understand and implement the subject matter described herein, and changes may be made to the function and arrangement of the elements discussed without departing from the scope of this specification. Various processes or components may be omitted, substituted, or added as needed in the examples. Furthermore, features described in some examples may be combined in other examples.

[0019] Please see Figure 1 , Figure 2 and Figure 3This invention discloses a production apparatus for a cement retarder used in cementing wells, comprising a reaction vessel unit 100, a circumferential mixing unit 200, a nitrogen distribution unit 300, a tiered turbulence unit 400, and an initiator injection unit 800. The reaction vessel unit 100 includes a vessel body 110, with a first feeding pipe 120 and a second feeding pipe 130 respectively disposed on the top of the vessel body 110, and a discharge port 140 disposed on the bottom of the vessel body 110. The circumferential mixing unit 200 includes a drive motor 210 fixedly installed on the top of the vessel body 110, and a rotating shaft 220 extending vertically into the vessel body 110 is installed at the output end of the drive motor 210. The lower end of the rotating shaft 220 is equipped with stirring blades 230; the nitrogen distribution unit 300 is disposed inside the rotating shaft 220 and rotates with the rotating shaft 220, nitrogen is introduced through the rotating shaft 220 and thrown out from the nitrogen distribution unit 300 into the liquid phase; the tiered turbulence unit 400 is disposed at the bottom of the vessel body 110, used to stir the bottom area of ​​the vessel body 110 to generate local turbulence and periodically push the accumulated material upward to the main stirring zone; the initiator injection unit 800 is disposed inside the rotating shaft 220 and rotates with the rotating shaft 220, initiator is introduced through the rotating shaft 220 and thrown out from the initiator injection unit 800 into the liquid phase; Specifically, 2-acrylamide-2-methylpropanesulfonic acid and maleic acid monomers are added to deionized water in reactor 110 through the first feed pipe 120 and the second feed pipe 130 respectively, according to a preset ratio. The stirring blades 230 at the lower end of the rotating shaft 220 are continuously rotated by the drive motor 210, thereby dispersing and stirring the mixed solution. Nitrogen gas and an initiator are continuously introduced into the liquid phase through independent channels within the rotating shaft 220, heating and continuously stirring the liquid phase to carry out the polymerization reaction, generating a polymer semi-finished product. Nitrogen gas enters the liquid phase from all directions from the bottom of reactor 110, and the bubbles rise in a spiral shape under centrifugal force, covering the entire cross-section of reactor 110. The shear force generated by the rotation can break down large bubbles into smaller bubbles, thereby creating a uniform bubble flow field throughout the reaction system and effectively avoiding residual dissolved oxygen in local areas. The initiator solution also enters the initiator injection unit 800 through the rotating shaft 220 and is sprayed into the liquid phase, so that the initiator and the reaction solution are quickly and uniformly mixed, avoiding the accumulation of initiator in local areas and the formation of insoluble gel particles due to rapid polymerization. During the nitrogen spraying process, the hierarchical turbulence unit 400 can be driven to move axially periodically. The generated local turbulence periodically throws the accumulated material upward and sends it into the main stirring zone, avoiding the deposition of high-viscosity polymer slurry at the bottom of the reactor 110 and causing batch-to-batch quality fluctuations.

[0020] It should be noted that the nitrogen distribution unit 300 is set inside the rotating shaft 220 and rotates with it. Nitrogen enters the liquid phase from the bottom of the vessel 110 from all directions. Under the action of centrifugal force, the bubbles rise in a spiral shape and cover the entire cross-section of the vessel 110. At the same time, the shear force generated by the rotation breaks the large bubbles into micro bubbles, forming a uniform and stable bubble flow field, avoiding the problem of local dissolved oxygen residue, effectively improving the deoxygenation effect of the polymerization reaction, avoiding the inhibition of free radical polymerization by oxygen, and ensuring the uniformity of the molecular weight and structure of the retarder. The initiator injection unit 800 rotates with the rotating shaft 220. The initiator solution is thrown out from the rotating unit through the independent channel inside the rotating shaft 220, achieving high-speed shear mixing with the reaction liquid. This avoids the instantaneous high concentration of the initiator in a local area, effectively preventing insoluble gel particles generated by rapid polymerization, thereby greatly improving the purity and dissolution stability of the product and ensuring the consistent flow properties of the cementing slurry. The hierarchical turbulence unit 400 is located at the bottom of the vessel 110 and is driven in conjunction with the nitrogen injection process to generate axial periodic motion. This motion can both stir the bottom area to form local turbulence and periodically push the deposited high-viscosity polymer slurry upward to the main stirring zone, avoiding the accumulation of materials in the dead corner of the bottom of the vessel in the high-viscosity reaction system and the batch-to-batch differences in molecular weight distribution and composition caused by deposition, thus effectively improving production reproducibility and product batch stability.

[0021] In one embodiment, please refer to Figure 4 and Figure 5 The nitrogen distribution unit 300 includes a nitrogen flow channel 310 axially opened within a rotating shaft 220. The lower end of the rotating shaft 220 is provided with an exhaust chamber 320 communicating with the nitrogen flow channel 310. The exhaust chamber 320 is provided with a plurality of inner exhaust grooves 321 circumferentially opened on its outer side. A support base 240 is fixed at the bottom inside the vessel body 110. The lower end of the rotating shaft 220 is rotatably embedded in the support base 240. The support base 240 is provided with a plurality of outer exhaust grooves 241 circumferentially opened to match the inner exhaust grooves 321. Specifically, nitrogen gas is continuously introduced into the exhaust chamber 320 through the nitrogen gas flow channel 310. When the rotating shaft 220 rotates, the inner exhaust groove 321 and the outer exhaust groove 241 are periodically staggered and connected, so that the nitrogen gas in the exhaust chamber 320 is periodically discharged into the liquid phase in the vessel body 110. At the same time, the periodic airflow can drive the hierarchical turbulence unit 400 to generate periodic movement, thereby achieving a periodic turbulence effect.

[0022] It is worth noting that when the rotating shaft 220 rotates, the internal exhaust groove 321 and the external exhaust groove 241 on the support base 240 are periodically staggered and connected, so that nitrogen is intermittently discharged into the liquid phase in a pulse manner. This periodic release method avoids the formation of large bubbles by continuous airflow. The airflow shear force generated by each pulse is stronger. Combined with the centrifugal effect of the rotating shaft 220, the bubbles can be broken into more uniform micro bubbles, which improves the gas-liquid contact area and dispersion efficiency, thereby removing dissolved oxygen in the reaction system more thoroughly. The periodic on / off of nitrogen gas is achieved entirely by the alignment change of the slot during the rotation of the shaft 220. The pulsed nitrogen gas generates a directional airflow impact at the moment of ejection. This periodic airflow directly serves as the driving force to trigger the hierarchical turbulence unit 400 to generate periodic motion. Compared with continuous airflow, pulsed airflow can generate a stronger instantaneous momentum change and more effectively drive the bottom accumulation material to be thrown upward. Since the internal exhaust groove 321 and the external exhaust groove 241 are evenly distributed in the circumferential direction, and nitrogen gas is periodically sprayed out from the bottom of the reactor body 110 at different angles as the rotating shaft 220 rotates, the bubble flow field is more evenly distributed across the entire cross-section of the reactor body 110, which in particular avoids dissolved oxygen residue in the area near the wall, thereby improving the batch consistency and product purity of the polymerization reaction.

[0023] Further, please refer to Figure 4 and Figure 5 The hierarchical turbulence unit 400 includes several sets of hinge seats 410 circumferentially distributed on the support base 240. A turbulence baffle 420 is rotatably mounted on the hinge seat 410. A flexible bladder 430 is provided outside the support base 240 to abut against the turbulence baffle 420. The interior of the flexible bladder 430 is connected to each external exhaust groove 241. An annular one-way valve plate 440 is provided at the bottom of the flexible bladder 430. The annular one-way valve plate 440 has several exhaust holes 441 circumferentially opened. Specifically, when the external exhaust channel 241 is connected to the internal exhaust channel 321, the nitrogen in the exhaust chamber 320 enters the flexible capsule 430 through the internal exhaust channel 321 and the external exhaust channel 241, causing the flexible capsule 430 to expand rapidly and instantaneously. This pushes the turbulence deflectors 420 upwards, using the raised turbulence deflectors 420 to axially propel and disturb the liquid phase. Subsequently, the external exhaust channel 241 and the internal exhaust channel 321 are staggered, and the nitrogen in the flexible capsule 430 is released into the liquid phase through the exhaust holes 441 at the bottom of the annular one-way valve plate 440. The flexible capsule 430 contracts, and the turbulence deflectors 420 swing back to their original position under the action of gravity. This process continues until the external exhaust channel 241 and the internal exhaust channel 321 are connected again to inflate the flexible capsule 430. This cycle repeats, achieving the periodic release of nitrogen and the periodic propulsion and turbulence effect of the flexible capsule 430.

[0024] It should be noted that the cyclic inflation and deflation of the flexible capsule 430 directly drives the turbulent flow baffle 420 to swing up and down around the hinge seat 410. The power transmission inside the flexible capsule 430 is accomplished solely through changes in nitrogen pressure. After entering the flexible capsule 430, the nitrogen first converts the pressure energy into mechanical energy to drive the turbulent flow baffle 420, thus axially pushing the material at the bottom. Subsequently, the nitrogen is slowly released into the liquid phase through the vent 441 at the bottom of the annular one-way valve plate 440, continuing to perform the deoxygenation function. The flexible capsule 430 expands rapidly and instantaneously, pushing the turbulence baffle 420 upward quickly, generating a strong upward thrust on the bottom area of ​​the vessel 110. When the flexible capsule 430 contracts, the turbulence baffle 420 swings back to its original position under the action of gravity, forming a downward auxiliary disturbance. This periodic axial pulse disturbance of rising and falling, combined with the tilt angle of the turbulence baffle 420 itself, can generate strong vortices and turbulence locally, effectively breaking the laminar boundary layer of the high-viscosity polymer slurry and forcibly throwing the bottom deposited material upward to the main stirring zone. The several vent holes 441 at the bottom of the annular one-way valve plate 440 allow nitrogen gas in the flexible bladder 430 to be slowly discharged from the bottom without causing liquid backflow into the flexible bladder 430. This directional release mechanism ensures that the flexible bladder 430 can contract uniformly and quickly after the vent grooves are staggered, avoiding the inability of the turbulent flow deflector 420 to fully reset due to residual gas pressure. At the same time, the throttling effect of the vent holes 441 ensures that the release process continues throughout the staggered cycle, ensuring that nitrogen gas enters the liquid phase in the form of uniform microbubbles, thus balancing the deoxygenation effect with the rhythm of the deflector action. Several sets of hinge seats 410 and turbulence baffles 420 are circumferentially distributed outside the support base 240. Each baffle is independently driven by the expansion of the flexible bladder 430. When the flexible bladder 430 expands, all baffles are pushed upward synchronously to form an annular flow surface around the bottom of the reactor body 110. This avoids flow dead zones caused by single-point or local disturbances and ensures that any material accumulation at any position at the bottom of the reactor body 110 can be periodically lifted, effectively eliminating the cone-bottom deposition phenomenon commonly seen in high-viscosity polymerization reactions.

[0025] In yet another embodiment, please refer to Figure 4 The initiator injection unit 800 includes an initiator flow channel 810 axially opened in the rotating shaft 220. The initiator flow channel 810 is distributed in parallel with the nitrogen flow channel 310, and a drain port 820 is provided at the lower end of the initiator flow channel 810. Please see Figure 2 and Figure 3 The top of the vessel body 110 is provided with a hollow sleeve 150, and the hollow sleeve 150 is provided with a gas supply component 330 that communicates with the nitrogen flow channel 310 and an injection component 830 that communicates with the initiator flow channel 810. Specifically, nitrogen is continuously supplied to the nitrogen flow channel 310 through the gas supply component 330, and initiator is continuously supplied to the initiator flow channel 810 through the injection component 830. Subsequently, the initiator flows through the initiator flow channel 810 to the drain port 820, and is thrown into the liquid phase from the drain port 820 under the centrifugal action of the rotating shaft 220.

[0026] Further, please refer to Figure 6 and Figure 7 The gas supply component 330 includes a gas supply chamber 331 disposed in the hollow sleeve 150. An air inlet pipe 332 is connected to one side of the gas supply chamber 331. A transition chamber 333 communicating with the nitrogen flow channel 310 is opened in the rotating shaft 220. A plurality of through holes 334 communicating with the interior of the gas supply chamber 331 are opened circumferentially on the outer side of the transition chamber 333. Please see Figure 6 and Figure 8 The injection component 830 includes an injection cavity 831 disposed in a hollow sleeve 150, an injection tube 832 connected to one side of the injection cavity 831, and an inlet 833 on the rotating shaft 220 that connects the initiator flow channel 810 and the injection cavity 831. Specifically, external high-pressure nitrogen is pumped into the gas supply chamber 331 through the air inlet pipe 332. Then, the nitrogen enters the transition chamber 333 through each through hole 334. Next, the nitrogen flows axially into the exhaust chamber 320 along the nitrogen flow channel 310, thereby realizing the uninterrupted supply of nitrogen to the liquid phase under the continuous rotation of the rotating shaft 220. Similarly, an external initiator is pumped into the injection chamber 831 through the injection pipe 832, and then the initiator enters the initiator flow channel 810 through the liquid inlet 833 until it is discharged into the liquid phase through the liquid outlet 820, so as to achieve uninterrupted supply of initiator to the liquid phase under the continuous rotation of the shaft 220.

[0027] It is worth noting that, through the cooperation of the gas supply chamber 331 and the transition chamber 333, the injection chamber 831 and the liquid inlet 833 provided in the hollow sleeve 150, nitrogen and initiator can still be continuously and stably input while the rotating shaft 220 is rotating at high speed. After the initiator flows through the initiator channel 810 to the drain port 820, it is accelerated and thrown into the liquid phase under the centrifugal force generated by the high-speed rotation of the rotating shaft 220. It is then pushed upward to the main stirring zone by the turbulent flow baffle 420 below, where it is broken into fine droplets by the stirring blades 230 and the turbulent flow field. This effectively shortens the time for the initiator to be uniformly distributed throughout the reactor from the injection point, further suppressing local overpolymerization. The nitrogen flow channel 310 and the initiator flow channel 810 are distributed in parallel and isolated from each other within the rotating shaft 220. They are supplied by independent gas supply components 330 and injection components 830, respectively. The two channels operate in parallel within the rotating component, which ensures that the two functions of nitrogen deoxygenation and initiator injection are carried out simultaneously, and avoids the risk of pipeline blockage that may be caused by premature mixing of nitrogen and initiator. Nitrogen gas in the gas supply chamber 331 enters the transition chamber 333 through several circumferentially opened through holes 334. No matter what angle the rotating shaft 220 rotates to, the through holes 334 are always connected to the gas supply chamber 331, thereby ensuring that the nitrogen flow is stable and without pulsation, avoiding possible periodic flow interruption, and enabling the nitrogen distribution unit 300 to continuously obtain a gas source, ensuring the continuity of the deoxygenation process.

[0028] In further embodiments, please refer to Figure 9 It also includes an anti-agglomeration impact unit 500 disposed above the stirring blade 230. The anti-agglomeration impact unit 500 includes several slide rails 510 circumferentially distributed on the inner wall of the vessel body 110. A lifting plate 520 is slidably mounted on the slide rails 510. An impact mesh 530 is disposed inside the lifting plate 520. A spiral sleeve 540 is fixedly sleeved on the rotating shaft 220. A spiral groove 550 is opened on the spiral sleeve 540. A locking pin 522 adapted to the spiral groove 550 is disposed on the lifting plate 520. Please see Figure 10 and Figure 11 The lifting plate 520 has a sliding cavity 521, and the locking pin 522 is radially slidably embedded in the sliding cavity 521; the lower end of the spiral groove 550 is provided with a magnetic block 523 adapted to the locking pin 522, and the upper end of the spiral groove 550 is provided with an impact hole 311 communicating with the nitrogen flow channel 310. Specifically, in the initial state, the lifting plate 520 is located at the lower end of the slide rail 510. At this time, the locking pin 522 is at the same height as the lower end of the spiral groove 550. The magnetic block 523 at the lower end of the spiral groove 550 has a magnetic attraction effect on the locking pin 522, thereby radially pulling the locking pin 522 out from the slide cavity 521, so that the locking pin 522 automatically locks into the spiral groove 550. As the rotating shaft 220 rotates, the locking pin 522 gradually moves upward along the spiral groove 550, thereby driving the lifting plate 520 to gradually rise along the slide rail 510. At the same time, the impact mesh 530 receives the powder discharged from the first feeding pipe 120 and the second feeding pipe 130 above. Until the lifting plate 520 rises to the top of the slide rail 510, the locking pin 522 just reaches the upper end of the spiral groove 550. Part of the nitrogen gas in the airflow channel 310 is ejected through the impact hole 311, thereby generating a radial impact on the locking pin 522, causing the locking pin 522 to retract into the sliding cavity 521. The locking pin 522 is passively moved out of the spiral groove 550, thereby releasing the connection between the lifting plate 520 and the spiral sleeve 540. The lifting plate 520 slides vertically downward under the action of gravity, thereby using the impact mesh 530 to impact the liquid surface below to break up the agglomerates floating on the liquid surface. At the same time, the impact mesh 530 vibrates the received powder into the liquid phase to achieve the periodic feeding of powder. Subsequently, the magnetic block 523 pulls the locking pin 522 out again and connects it to the spiral groove 550, so that the lifting plate 520 rises again with the rotating shaft 220. This process is repeated to achieve the periodic lifting and lowering movement of the lifting plate 520.

[0029] It is worth noting that when the lifting plate 520 falls vertically from the top of the slide rail 510 under the action of gravity, its built-in impact mesh 530 impacts the liquid surface at a certain speed, generating an instantaneous shock wave. This impact force can effectively break up the agglomerates formed on the liquid surface due to the powder absorbing moisture or electrostatic effects, and at the same time force the light floating particles to be pressed below the liquid surface. This periodic falling impact method has a stronger destructive force on the agglomerates on the high viscosity liquid surface, avoiding the incomplete reaction caused by the long-term floating of powder agglomerates or the appearance of fish-eye-shaped insoluble matter in the product. During the upward movement of the lifting plate 520, the impact mesh 530 is located directly below the outlets of the first feeding pipe 120 and the second feeding pipe 130, which can receive the powder and allow the powder to be evenly spread on the mesh beforehand. When the lifting plate 520 falls and impacts the liquid surface, the powder on the mesh is instantly shaken off and immersed into the depth of the liquid phase along with the shock wave. This avoids the formation of clumps or cores due to excessively high local concentration when the powder is poured directly, and effectively improves the initial contact uniformity between the powder and the liquid. When the locking pin 522 reaches the upper end of the spiral groove 550, part of the high-pressure nitrogen in the nitrogen flow channel 310 is precisely ejected through the impact hole 311, generating a radial impact force on the locking pin 522. This overcomes the attraction of the magnetic block 523 and pushes the locking pin 522 back into the sliding cavity 521. At the same time, the position of the impact hole 311 is strictly aligned with the end point of the spiral groove 550, ensuring the timing accuracy of the release and preventing the locking pin 522 from jamming or disengaging prematurely. The impact cycle is directly related to the rotational speed of the shaft 220. In the early stage of the reaction when the material viscosity is low, a higher rotational speed can be used to increase the impact frequency, which helps the powder to disperse quickly. In the later stage of the reaction when the viscosity increases, the rotational speed can be reduced to reduce the number of impacts and avoid excessive disturbance. After the lifting plate 520 falls to the bottom, the locking pin 522 and the magnetic block 523 at the lower end of the spiral groove 550 are realigned. The magnetic force automatically pulls the locking pin 522 out of the sliding cavity 521 and into the spiral groove 550, preparing for the next rise. When the impact mesh 530 rises, it acts as a powder support platform, using the mesh openings to allow fine powder to fall down in advance, retaining only larger particles that may agglomerate. When it falls and impacts, the mesh also acts as a crushing tool to cut and disperse large clumps. In addition, during the reaction process, the mesh moves up and down with the lifting plate 520, which can also intercept and break up the polymer microgels in the upper liquid phase, playing an auxiliary role in homogenization.

[0030] Further, please refer to Figure 3 and Figure 12 Above the anti-agglomeration impact unit 500, a powder feeding unit 600 is also provided. The powder feeding unit 600 includes a conical guide plate 610 fixed on the inner wall of the reactor body 110. A ring-shaped collecting plate 620 is horizontally arranged at the lower end of the conical guide plate 610. A mounting bracket 630 is fixed on the rotating shaft 220. A comb tooth 640 adapted to the ring-shaped collecting plate 620 is provided at the end of the mounting bracket 630 away from the rotating shaft 220. Specifically, the conical guide plate 610 guides the powder falling from the first feeding pipe 120 and the second feeding pipe 130, causing the powder to slide down the inclined conical guide plate 610 onto the horizontal annular collecting plate 620. At the same time, the comb teeth 640 rotate synchronously with the rotating shaft 220, thereby combing and spreading the powder accumulated on the annular collecting plate 620. As the powder gradually accumulates on the annular collecting plate 620, the combed powder can fall down from the inside of the annular collecting plate 620 onto the impact mesh 530, so as to achieve uniform feeding of the powder.

[0031] It should be noted that the conical guide plate 610 guides the powder falling from the first feeding pipe 120 and the second feeding pipe 130 along the inclined surface to the annular collecting plate 620, avoiding local accumulation caused by the direct vertical fall of the powder; the powder stays briefly on the annular collecting plate 620, and after being combed and spread evenly by the comb teeth 640, it falls evenly and slowly from the inner edge to the impact mesh 530 below, effectively reducing the instantaneous powder concentration per unit area and inhibiting the formation of agglomerates from the source; The mounting frame 630 rotates with the rotating shaft 220, driving the comb teeth 640 to move circumferentially along the annular collecting plate 620. The toothed structure of the comb teeth 640 can break up and flatten the accumulated powder, and force the powder to move towards the inner opening. Compared with the method of relying on gravity to slide naturally, this active mechanical combing overcomes the adhesion and bridging phenomenon caused by moisture or static electricity, ensuring a stable and continuous discharge rate. By adjusting the width of the annular collecting plate 620, the spacing of the comb teeth 640, and the rotation speed of the rotating shaft 220, the residence time and accumulation thickness of the powder on the collecting plate can be controlled. For fine powder that is prone to agglomeration or for high feeding rate conditions, the rotation speed can be increased to speed up spreading and discharge. For powder with poor flowability, the rotation speed can be reduced to extend the spreading time. The powder falls from the inner side of the annular collecting plate 620 directly opposite the impact mesh 530 below, and the impact mesh 530 is in a periodic rising and falling state. When the impact mesh 530 rises, its surface approaches or receives the falling powder, so that the powder forms a thin layer of pre-distribution on the mesh. When the impact mesh 530 falls and impacts the liquid surface, the powder on the mesh is shaken apart and forcibly immersed, realizing the fine control of the powder from entering the reactor 110 to mixing into the liquid phase, and greatly reducing the probability of local agglomeration.

[0032] Furthermore, please refer to Figure 4 and Figure 13 The discharge outlet 140 is provided with a discharge unit 700, the discharge unit 700 includes a discharge pipe 710 rotatably installed in the discharge outlet 140, the upper end of the discharge pipe 710 is provided with a plurality of inner discharge ports 711, and the bottom of the support base 240 is provided with a plurality of outer discharge ports 242 adapted to the inner discharge ports 711. Specifically, in the initial state, the inner discharge port 711 and the outer discharge port 242 are staggered to block the discharge pipe 710; when discharge is required, the discharge pipe 710 is rotated to connect the inner discharge port 711 and the outer discharge port 242, so that the liquid phase in the vessel body 110 can be discharged into the discharge pipe 710 through the outer discharge port 242 and the inner discharge port 711.

[0033] It should be noted that by rotating the discharge pipe 710, the inner discharge port 711 and the outer discharge port 242 are switched from a completely staggered blocked state to a completely connected discharge state; when connected, multiple circumferentially distributed orifices open simultaneously to form an annular discharge channel, which can quickly discharge high-viscosity polymer slurry and avoid stringing or blockage caused by excessive local flow velocity. Several internal discharge ports 711 and external discharge ports 242 are evenly distributed circumferentially. During discharge, liquid phase is simultaneously drawn from multiple positions around the bottom of the vessel body 110, avoiding the flow deviation caused by the material accumulation angle when discharging through a single port. For high-viscosity polymers, simultaneous discharge through multiple ports can form a uniform radial flow field, carrying out the material deposited around the bottom, reducing the amount of material residue between batches and improving product yield. In the initial state, the inner discharge port 711 and the outer discharge port 242 are completely offset and require a clear rotational action to connect. They will not open automatically due to accidental contact or pipeline pressure fluctuations. This is especially suitable for situations where the bottom of the reactor 110 needs to be strictly sealed during the polymerization reaction to prevent premature leakage of high-temperature materials and potential safety accidents.

[0034] The present invention also provides a production method using a production apparatus for cementing oil well cement retarder, comprising the following steps: Step 1: Add 2-acrylamide-2-methylpropanesulfonic acid and maleic acid monomers to the deionized water in the reactor body 110 through the first feed pipe 120 and the second feed pipe 130 respectively in a preset ratio; Step 2: Start the drive motor 210 to drive the stirring blades 230 at the lower end of the rotating shaft 220 to rotate continuously, and disperse and stir the mixed solution; Step 3: Nitrogen gas is continuously introduced into the liquid phase through the independent channel inside the rotating shaft 220. The nitrogen gas enters from all directions from the bottom of the vessel 110 and rises spirally to form a uniform bubble flow field to remove local dissolved oxygen residue. Step 4: Inject the initiator solution into the liquid phase through the independent channel inside the rotating shaft 220 to ensure rapid and uniform mixing and avoid local enrichment that could lead to the formation of insoluble gel particles. Step 5: The liquid phase is heated and continuously stirred to carry out the polymerization reaction, generating a polymer semi-finished product; Step 6: During the nitrogen injection process, the hierarchical turbulence unit 400 is driven to move axially and periodically, throwing the bottom accumulated material upward into the main stirring zone to prevent the deposition of high-viscosity slurry.

[0035] The specific embodiments of the present invention have been described above. However, the present invention is not limited to the specific embodiments described above. The specific embodiments described above are merely illustrative and not restrictive. Those skilled in the art can make many other forms under the guidance of the present invention, all of which are within the protection scope of the present invention.

Claims

1. A production apparatus for a cement retarder for well cementing, characterized in that, include: The reactor unit (100) includes a reactor body (110), the top of which is provided with a first feeding pipe (120) and a second feeding pipe (130), and the bottom of which is provided with a discharge port (140). A circumferential mixing unit (200) includes a drive motor (210) fixedly installed on the top of the vessel body (110), and a rotating shaft (220) extending vertically into the vessel body (110) is installed at the output end of the drive motor (210), and a stirring blade (230) is installed at the lower end of the rotating shaft (220). A nitrogen distribution unit (300) is disposed inside a rotating shaft (220) and rotates together with the rotating shaft (220). Nitrogen gas is introduced through the rotating shaft (220) and ejected from the nitrogen distribution unit (300) into the liquid phase. A tiered turbulence unit (400) is located at the bottom of the vessel body (110) to agitate the bottom region of the vessel body (110) to generate local turbulence and periodically push the accumulated material upward to the main stirring zone; The initiator injection unit (800) is located inside the rotating shaft (220) and rotates together with the rotating shaft (220). The initiator is introduced through the rotating shaft (220) and ejected from the initiator injection unit (800) into the liquid phase.

2. The production apparatus for a cement retarder for well cementing according to claim 1, characterized in that, The nitrogen distribution unit (300) includes a nitrogen flow channel (310) axially opened in a rotating shaft (220). The lower end of the rotating shaft (220) is provided with an exhaust chamber (320) communicating with the nitrogen flow channel (310). The exhaust chamber (320) is provided with a plurality of inner exhaust grooves (321) circumferentially opened on the outer side. The bottom of the vessel body (110) is fixed with a support base (240). The lower end of the rotating shaft (220) is rotatably embedded in the support base (240). The support base (240) is provided with a plurality of outer exhaust grooves (241) circumferentially opened on the support base (240) that are adapted to the inner exhaust grooves (321).

3. The production apparatus for a cement retarder for well cementing according to claim 2, characterized in that, The hierarchical turbulence unit (400) includes several sets of hinge seats (410) circumferentially distributed on the support base (240). A turbulence baffle (420) is rotatably mounted on the hinge seat (410). A flexible bladder (430) is provided on the outside of the support base (240) and abuts against the turbulence baffle (420). The interior of the flexible bladder (430) is connected to each external exhaust groove (241). An annular one-way valve plate (440) is provided at the bottom of the flexible bladder (430). A number of exhaust holes (441) are opened circumferentially on the annular one-way valve plate (440).

4. The production apparatus for a cement retarder for well cementing according to claim 2, characterized in that, The initiator injection unit (800) includes an initiator flow channel (810) axially opened in the rotating shaft (220), the initiator flow channel (810) is distributed in parallel with the nitrogen flow channel (310), and a drain port (820) is provided at the lower end of the initiator flow channel (810). The top of the vessel body (110) is provided with a hollow sleeve (150), and the hollow sleeve (150) is provided with a gas supply component (330) communicating with the nitrogen flow channel (310) and an injection component (830) communicating with the initiator flow channel (810).

5. The production apparatus for a cement retarder for well cementing according to claim 4, characterized in that, The gas supply component (330) includes a gas supply chamber (331) disposed in a hollow sleeve (150), an air inlet pipe (332) connected to one side of the gas supply chamber (331), a transition chamber (333) communicating with the nitrogen flow channel (310) is provided in the rotating shaft (220), and a plurality of through holes (334) communicating with the interior of the gas supply chamber (331) are provided circumferentially on the outer side of the transition chamber (333). The injection component (830) includes an injection cavity (831) disposed in a hollow sleeve (150), an injection tube (832) is connected to one side of the injection cavity (831), and an inlet (833) is provided on the rotating shaft (220) to connect the initiator flow channel (810) and the injection cavity (831).

6. The production apparatus for a cement retarder for well cementing according to claim 1, characterized in that, It also includes an anti-agglomeration impact unit (500) disposed above the stirring blade (230). The anti-agglomeration impact unit (500) includes several slide rails (510) circumferentially distributed on the inner wall of the vessel body (110). A lifting plate (520) is slidably installed on the slide rails (510). An impact mesh (530) is disposed inside the lifting plate (520). A spiral sleeve (540) is fixedly sleeved on the rotating shaft (220). A spiral groove (550) is opened on the spiral sleeve (540). A locking pin (522) adapted to the spiral groove (550) is provided on the lifting plate (520).

7. The production apparatus for a cement retarder for well cementing according to claim 6, characterized in that, The lifting plate (520) has a sliding cavity (521) inside, and the locking pin (522) is radially slidably embedded in the sliding cavity (521); the lower end of the spiral groove (550) is provided with a magnetic block (523) that matches the locking pin (522), and the upper end of the spiral groove (550) is provided with an impact hole (311) that communicates with the nitrogen flow channel (310).

8. The production apparatus for a cement retarder for well cementing according to claim 6, characterized in that, Above the anti-agglomeration impact unit (500) is a powder feeding unit (600). The powder feeding unit (600) includes a conical guide plate (610) fixed on the inner wall of the vessel body (110). A ring-shaped collecting plate (620) is horizontally arranged at the lower end of the conical guide plate (610). A mounting bracket (630) is fixed on the rotating shaft (220). A comb tooth (640) adapted to the ring-shaped collecting plate (620) is provided at the end of the mounting bracket (630) away from the rotating shaft (220).

9. A production apparatus for a cement retarder for well cementing according to claim 2, characterized in that, A discharge unit (700) is provided at the discharge port (140). The discharge unit (700) includes a discharge pipe (710) rotatably installed in the discharge port (140). The upper end of the discharge pipe (710) is provided with a plurality of inner discharge ports (711) and the bottom of the support base (240) is provided with a plurality of outer discharge ports (242) adapted to the inner discharge ports (711).

10. A production method using a production apparatus for cementing oil well cement retarder according to any one of claims 1-9, characterized in that, Includes the following steps: Step 1: Add 2-acrylamide-2-methylpropanesulfonic acid and maleic acid monomers to the deionized water in the reactor body (110) through the first feeding pipe (120) and the second feeding pipe (130) respectively in a preset ratio; Step 2: Start the drive motor (210) to drive the stirring blades (230) at the lower end of the rotating shaft (220) to rotate continuously, and disperse and stir the mixed solution; Step 3: Nitrogen gas is continuously introduced into the liquid phase through the independent channel inside the rotating shaft (220). The nitrogen gas enters from all directions from the bottom of the vessel body (110) and spirals upward to form a uniform bubble flow field to remove local dissolved oxygen residue. Step 4: Inject the initiator solution into the liquid phase through the independent channel inside the rotating shaft (220) to make it mix quickly and evenly, and avoid local enrichment to prevent the formation of insoluble gel particles; Step 5: The liquid phase is heated and continuously stirred to carry out the polymerization reaction, generating a polymer semi-finished product; Step 6: During the nitrogen injection process, the hierarchical turbulence unit (400) is driven to move axially and periodically to throw the bottom accumulated material upward into the main stirring zone to prevent the deposition of high viscosity slurry.

Images