A reaction tower, emulsifier continuous production system and method

Abstract

The present application belongs to the field of emulsifier production, and relates to a reaction tower, an emulsifier continuous production system and method. The reaction tower is internally provided with a plurality of tube bank sections and filler sections; the tube bank sections are sequentially provided from top to bottom with a perforated plate distributor, a membrane distributor, a tube sheet and a reaction tube; and the filler section comprises filler and a cylindrical cylinder. The emulsifier continuous production method provided by the present application comprises: after preheated oleic acid is mixed with diethylenetriamine, the mixture is fed into a primary reaction tower for reaction, a first product obtained at the bottom of the tower is partially fed into a secondary reaction tower for continuous reaction to obtain a second product, and the other part of the first product and the second product are respectively cooled and mixed, and then mixed with oleic acid and white oil to continuously obtain a product emulsifier. The emulsifier continuous production system and method have the advantages of scientific and reasonable process, high production efficiency, low operation cost, small safety risk, stable product quality, easy scale production and the like, and have high innovation.

Description

Technical Field

[0001] The present invention belongs to the technical field of emulsifier production, and in particular relates to a reaction tower, an emulsifier continuous production system and a method. Background Art

[0002] In the high-temperature environment of deep oil and gas reservoir drilling, the molecular activity of the oil-based drilling fluid emulsifier increases, the probability of emulsifier molecule breakage increases, and the interaction force between molecules is reduced, causing the emulsifier to lose its emulsifying ability, thereby destroying the rheological properties and wall protection ability of the oil-based drilling fluid.

[0003] In order to solve the problem of high temperature resistance of emulsifiers and avoid high temperature failure of emulsifiers, a new type of high-end emulsifier has been developed. It relies on intermolecular forces to improve its emulsification performance, and increases the intramolecular rigidity to create steric hindrance, thereby enhancing its high temperature resistance.

[0004] This emulsifier currently utilizes a traditional kettle reaction process, which results in large reactor volumes, small heat exchange areas, and inconsistent residence times. Furthermore, the material's high viscosity creates significant diffusion resistance for byproducts within the system. To increase the diffusion rate of byproducts, the existing process requires the introduction of water-carrying agents (flammable and explosive organic compounds), increasing production risks. Overall, production is time-consuming, energy-intensive, and costly, and can be subject to capacity constraints.

[0005] Therefore, designing a process and reaction device that can realize the continuous production of new high-end emulsifiers is of great significance for improving production efficiency, reducing production costs, and improving production conditions. Summary of the Invention

[0006] The purpose of the present invention is to provide a reaction tower, an emulsifier continuous production system and a method for the defects of the prior art.

[0007] Specifically, the reaction tower provided by the present invention includes a tower top, a tower body and a tower bottom, wherein a plurality of tube sections and packing sections are arranged inside the tower body;

[0008] The tube array section includes a cylindrical body and a perforated plate distributor, a membrane distributor, a tube sheet, and a reaction tube arranged in sequence from top to bottom inside the cylindrical body. The cylindrical body is provided with a heat medium outlet and a heat medium inlet in sequence from top to bottom.

[0009] The packing section includes a packing and a cylindrical body, wherein the packing is a corrugated plate arranged regularly and vertically.

[0010] In the above-mentioned reaction tower, the reaction tube is a seamless tube with a surface spiral structure or a corrugated structure.

[0011] In the above-mentioned reaction tower, the orifice plate distributor is an orifice plate with a cofferdam, and the holes are staggered with the reaction tubes.

[0012] The reaction tower, the upper end of the reaction tube is sawtooth or square groove structure.

[0013] The reaction tower, the outer packing section is provided with a jacket.

[0014] In another aspect, the present application provides a continuous production system of emulsifier, comprising: preheater, first mixer, primary reaction tower, secondary reaction tower, second mixer, third mixer and third cooler connected in sequence;

[0015] The primary reaction tower and the secondary reaction tower are the reaction tower, and the top of the tower is connected with a vacuum system;

[0016] The outlet of the primary reaction tower and the secondary reaction tower is connected with the inlet of the first cooler and the second cooler respectively, and the outlet of the first cooler and the second cooler is connected with the inlet of the second mixer.

[0017] In another aspect, the present application also provides a continuous production method of emulsifier, comprising: after the preheated oleic acid is mixed with diethylene triamine, the mixture is sent into the primary reaction tower for reaction, the first product obtained at the bottom of the tower is partly sent into the secondary reaction tower for further reaction to obtain the second product, and the other part of the first product and the second product are mixed after cooling, and the mixture is mixed with oleic acid and white oil to continuously obtain the product emulsifier.

[0018] The continuous production method of emulsifier is carried out by using the continuous production system of emulsifier, comprising:

[0019] (1) the oleic acid is preheated in the preheater and then sent into the first mixer;

[0020] (2) the diethylene triamine is added into the first mixer to mix with the preheated oleic acid to obtain the raw material;

[0021] (3) the raw material is sent into the primary reaction tower for reaction, part of the first product is sent into the secondary reaction tower for further reaction to obtain the second product, and the other part of the first product is sent into the first cooler for cooling;

[0022] (4) the second product is cooled in the second cooler, and then mixed with the cooled first product in the second mixer, and then mixed with the oleic acid and white oil in the third mixer;

[0023] (5) the mixture in the third mixer is sent into the third cooler for cooling to obtain the product emulsifier.

[0024] The continuous production method of emulsifier, the discharge temperature at the bottom of the primary reaction tower is 140-190℃.

[0025] In the above-mentioned continuous emulsifier production method, the discharge temperature at the bottom of the secondary reaction tower is 190-250°C.

[0026] In the above-mentioned continuous emulsifier production method, the vacuum degree in the first-stage reaction tower and the second-stage reaction tower is 5-75 kPa.

[0027] The technical solution of the present invention has the following beneficial effects:

[0028] (1) The reaction tower of the present invention adopts a combination of a tubular section and a packing section. Compared with ordinary tubular reactors, the packing has a much larger specific surface area. When the material flows along the packing surface in the packing section, the reaction area is large and the residence time is long, which can effectively reduce the height of the tower, thereby reducing equipment costs.

[0029] (2) The reaction tower of the present invention has a scientific and reasonable process and has the advantages of high production efficiency, low operating cost, low safety risk, and stable product quality. It is a highly innovative reactor for continuous production of emulsifiers.

[0030] (3) Conventional packed towers as reactors can only transfer heat through jackets, resulting in a small heat transfer area and low heat transfer efficiency. When the reaction tower of the present invention is used to produce emulsifiers, the material flows in a film-like manner along the interior of the heat exchange tubes in the tube section, which not only improves the heat transfer efficiency and reduces the mass transfer resistance, but also provides space and channels for the vaporization of by-products, allowing the by-products to quickly leave the system, making continuous production of emulsifiers possible and greatly improving the reaction speed;

[0031] (4) The continuous emulsifier production system of the present invention not only improves the automation level and realizes unmanned operation while ensuring stable product quality, but also realizes continuous production of emulsifiers, greatly improves production efficiency and reduces production costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Various other advantages and benefits will become apparent to those skilled in the art by reading the following detailed description of the preferred embodiment.The accompanying drawings are only for the purpose of illustrating the preferred embodiment and are not to be considered as limiting the present invention.

[0033] Figure 1 This is the main view of the reaction tower;

[0034] Figure 2 for Figure 1 BB cross-sectional view (packing section, without jacket);

[0035] Figure 3 This is the main view of the reaction tube with a surface spiral structure;

[0036] Figure 4 This is the main view of the corrugated structure reaction tube;

[0037] Figure 5 for Figure 1 AA cross-sectional view (distributor);

[0038] Figure 6 This is a schematic diagram of the structure of the packing section with a jacket;

[0039] Figure 7 This is a continuous production process flow chart.

[0040] Description of reference numerals:

[0041] 1 is the tower top, 11 is the head, 12 is the demister, 13 is the steam outlet, 14 is the head box, 15 is the feed pipe, and 16 is the nozzle; 2 is the tower body, 211 is the orifice distributor, 212 is the membrane distributor, 213 is the tube sheet, 214 is the reaction tube, 215 is the heat medium outlet, 216 is the heat medium inlet, 217 is the cylindrical body, 2111 is the cofferdam, 2112 is the hole, 221 is the packing, 222 is the cylindrical body, 223 is the jacket, 224 is the heat medium outlet of the packing section, and 225 is the heat medium inlet of the packing section; 3 is the tower bottom, 31 is the tower kettle, 32 is the discharge pipe, and 4 is the flange. DETAILED DESCRIPTION

[0042] In order to fully understand the purpose, features and effects of the present invention, the present invention is described in detail through the following specific embodiments. Except for the following contents, the process of the present invention adopts conventional methods or devices in the art. Unless otherwise specified, the following terms have the meanings commonly understood by those skilled in the art.

[0043] Specifically, such as Figure 1 As shown, the reaction tower of the present invention comprises a tower top 1, a tower body 2 and a tower bottom 3, wherein a plurality of tube sections 21 and a packing section 22 are provided inside the tower body 2;

[0044] The tube array section 21 includes a cylindrical body 217 and an orifice plate distributor 211, a film distributor 212, a tube sheet 213, and a reaction tube 214 arranged in sequence from top to bottom inside the cylindrical body. The cylindrical body 217 is provided with a heat medium outlet 215 and a heat medium inlet 216 in sequence from top to bottom.

[0045] The packing section 22 includes a packing 221 and a cylindrical body 222, wherein the packing is a regular, vertically arranged corrugated plate (such as Figure 2 ).

[0046] The reaction tower of the present invention utilizes a rational combination of tubing sections 21 and packing sections 22, allowing material to flow in a film-like manner along the interior of the heat exchange tubes within tubing sections 21, achieving both efficient heat transfer and reduced mass transfer resistance. The packing utilizes regular, vertically arranged corrugated plates 221, significantly increasing the specific surface area. As material flows along the packing surface within packing section 22, the reaction area is large and the residence time is prolonged. Compared to conventional tubular reactors, the present invention significantly increases the reaction area and residence time, allowing for a significant reduction in tower height and equipment cost.

[0047] In some preferred embodiments, the reaction tube 214 is a seamless tube with a spiral or corrugated surface structure (e.g. Figure 3 and Figure 4 The use of a reaction tube or bellows with a spiral structure processed by pressure is conducive to film formation of the liquid in the reaction tube, and increases the turbulence effect of the liquid, which is beneficial to heat transfer and diffusion of by-products.

[0048] The tube section 21 and the filler section 22 are fixedly connected via a flange 4 .

[0049] Among them, such as Figure 5 As shown, the orifice plate distributor 211 is a orifice plate with a cofferdam 2111 , and the holes 2112 are staggered with the reaction tube 214 , thereby evenly distributing the reaction raw materials on the surface of the reaction tube 214 .

[0050] The upper end of the reaction tube 214 is a sawtooth or square groove structure.

[0051] In some optional embodiments, a tube segment 21 is provided at the top of the tower body 2 of the reaction tower, and 1-10 tube segments 21 and / or packing segments 22 are provided below the tube segment 21 .

[0052] In actual production, the number and assembly sequence of the tube sections 21 and the packing sections 22 can be flexibly adjusted according to different processing volumes and usage requirements, thereby meeting different operating conditions and improving the adaptability of the reaction tower.

[0053] In some preferred embodiments, Figure 6 As shown, a jacket 223 is provided outside the packing section 22, a packing section heat medium outlet 224 is provided above the jacket, and a packing section heat medium inlet 225 is provided below the jacket.

[0054] In some other preferred embodiments, Figure 1 As shown, the top 1 of the reaction tower includes: a head 11, a demister 12, a steam outlet 13, a head pipe box 14, a feed pipe 15, and a nozzle 16; the bottom 3 of the reaction tower includes a kettle 31 and a discharge pipe 32.

[0055] The head 11, the head pipe box 14, the tube segment 21, the packing segment 22 and the tower kettle 31 are coaxially installed, the steam outlet 13 is arranged at the middle position of the head 11, the demister 12 is arranged at the upper portion in the head pipe box 14, the feed pipe 15 is arranged on the head pipe box 14 and extends to the center line, and the spray head 16 is connected to the end of the feed pipe 15.

[0056] The present application can ensure the distribution effect of the material by adopting the two-stage distribution mode of the spray head 16 and the orifice plate distributor 211.

[0057] On the other hand, as Figure 7 The emulsifier continuous production system provided by the present application comprises, sequentially connected, a preheater, a first mixer, a first-stage reaction tower, a second-stage reaction tower, a second mixer, a third mixer and a third cooler.

[0058] The first-stage reaction tower and the second-stage reaction tower are the reaction towers described above, and the top of each is connected with a vacuum system.

[0059] The outlet of the first-stage reaction tower and the second-stage reaction tower is respectively connected with the inlet of a first cooler and a second cooler, and the outlet of the first cooler and the second cooler is connected with the inlet of the second mixer.

[0060] The emulsifier continuous production system provided by the present application not only improves the automation level and realizes unattended operation, but also realizes the continuous production of the emulsifier, greatly improves the production efficiency and reduces the production cost, under the premise of ensuring the stable product quality.

[0061] In another aspect, the present application provides an emulsifier continuous production method, which comprises: after the preheated oleic acid is mixed with diethylene triamine, the mixture is sent into a first-stage reaction tower for reaction, a first product obtained at the bottom of the tower is partly sent into a second-stage reaction tower for continuous reaction to obtain a second product, and the other part of the first product and the second product are mixed after being cooled respectively, and then mixed with oleic acid and white oil to continuously obtain a product emulsifier.

[0062] Preferably, as Figure 7 The emulsifier continuous production method provided by the present application is carried out by using the emulsifier continuous production system described above, and comprises:

[0063] (1) The oleic acid is preheated in a preheater and then sent into a first mixer;

[0064] (2) The diethylene triamine is added into the first mixer to be mixed with the preheated oleic acid to obtain raw materials;

[0065] (3) After the raw materials are sent into the first-stage reaction tower for reaction, a part of the first product is sent into the second-stage reaction tower for continuous reaction to obtain the second product, and the other part of the first product is sent into a first cooler for cooling.

[0066] (4) the second product is passed into a second cooler to be cooled and then mixed with the cooled first product in a second mixer, and then passed into a third mixer to be mixed with oleic acid and white oil;

[0067] (5) The mixture in the third mixer is sent to the third cooler for cooling to obtain a product emulsifier.

[0068] Preferably, the discharge temperature at the bottom of the primary reaction tower is 140-190°C; the discharge temperature at the bottom of the secondary reaction tower is 190-250°C; and the vacuum degree in the primary reaction tower and the secondary reaction tower is 5-75kPa, thereby ensuring the smooth continuous production of the emulsifier.

[0069] The continuous emulsifier production method of the present invention solves the problems of long reaction time, low efficiency and high energy consumption in existing intermittent production technology, has the advantages of high production efficiency, low operating cost, low safety risk and stable product quality, and is a highly innovative continuous emulsifier production process.

[0070] The present invention has been disclosed above with reference to preferred embodiments. However, those skilled in the art will appreciate that these embodiments are intended only to illustrate the present invention and are not to be construed as limiting the scope of the present invention. It should be noted that any equivalent variations and substitutions to these embodiments are to be considered encompassed within the scope of the claims of the present invention. Therefore, the scope of protection of the present invention shall be subject to the scope defined in the claims.

[0071] The terms "first", "second", etc. used herein do not indicate any order or importance, but are used to distinguish one element from another. The terms "the", "said", "a", and "an" do not indicate a limitation on quantity, but rather indicate the presence of at least one of the objects mentioned. The terms "preferred", "more preferred", etc. refer to embodiments of the present invention that may provide certain beneficial effects in certain circumstances. However, other embodiments may also be preferred under the same circumstances or other circumstances. In addition, the description of one or more embodiments does not imply that other embodiments are not applicable, nor is it intended to exclude other embodiments from the scope of the present invention.

[0072] When a numerical range is disclosed herein, the range is considered continuous and includes the minimum and maximum values ​​of the range, as well as every value between such minimum and maximum values. Further, when a range refers to an integer, every integer between the minimum and maximum values ​​of the range is included. In addition, when multiple ranges are provided to describe a feature or characteristic, the ranges can be combined. In other words, unless otherwise indicated, all ranges disclosed herein are understood to include any and all subranges subsumed therein.

Claims

1. A reaction tower comprising a tower top, a tower body and a tower bottom, characterized in that: A plurality of tube sections and filler sections are provided inside the tower body; The tube array section includes a cylindrical body and a perforated plate distributor, a membrane distributor, a tube sheet, and a reaction tube arranged in sequence from top to bottom inside the cylindrical body. The cylindrical body is provided with a heat medium outlet and a heat medium inlet in sequence from top to bottom. The packing section includes a packing and a cylindrical body, wherein the packing is a corrugated plate arranged regularly and vertically.

2. The reaction tower according to claim 1, characterized in that The reaction tube is a seamless tube with a spiral structure or a corrugated structure on the surface.

3. The reaction tower according to claim 1, characterized in that The orifice plate distributor is an orifice plate with a cofferdam, and the holes are staggered with the reaction tubes.

4. The reaction tower according to claim 1, characterized in that The upper end of the reaction tube is a sawtooth or square groove structure.

5. The reaction tower according to claim 1, characterized in that A jacket is provided outside the packing section.

6. A continuous emulsifier production system, characterized in that: include: A preheater, a first mixer, a primary reaction tower, a secondary reaction tower, a second mixer, a third mixer and a third cooler connected in sequence; The primary reaction tower and the secondary reaction tower are the reaction towers according to any one of claims 1 to 5, and the tops of the towers are both connected to a vacuum system; The outlets of the primary reaction tower and the secondary reaction tower are connected to the inlets of a first cooler and a second cooler, respectively, and the outlets of the first cooler and the second cooler are connected to the inlet of the second mixer.

7. A continuous production method for an emulsifier, characterized in that: include: After the preheated oleic acid is mixed with diethylenetriamine, it enters the primary reaction tower for reaction. A portion of the first product obtained at the bottom of the tower enters the secondary reaction tower for further reaction to obtain the second product. The other portions of the first product and the second product are cooled separately and then mixed. Oleic acid and white oil are then added for mixing to continuously obtain the product emulsifier.

8. The continuous production method of emulsifier according to claim 7, characterized in that: The continuous emulsifier production system according to claim 6 is used, comprising: (1) passing oleic acid into a preheater for preheating and then feeding it into a first mixer; (2) adding diethylenetriamine into a first mixer and mixing it with preheated oleic acid to obtain a raw material; (3) After the raw materials are passed into the primary reaction tower to participate in the reaction, a portion of the first product is passed into the secondary reaction tower to continue the reaction to obtain the second product, and the other portion of the first product is passed into the first cooler for cooling; (4) the second product is passed into a second cooler to be cooled and then mixed with the cooled first product in a second mixer, and then passed into a third mixer to be mixed with oleic acid and white oil; (5) The mixture in the third mixer is sent to the third cooler for cooling to obtain a product emulsifier.

9. The continuous production method of emulsifier according to claim 7, characterized in that: The discharge temperature of the bottom of the primary reaction tower is 140-190°C; the discharge temperature of the bottom of the secondary reaction tower is 190-250°C.

10. The continuous production method of emulsifier according to claim 7, characterized in that: The vacuum degree in the primary reaction tower and the secondary reaction tower is 5-75 kPa.

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