TWM506148U - Tubular reactor for nylon synthesis with improved design - Google Patents

Abstract

The present invention relates to methods, systems, and apparatus for making polyamides having at least two heat-transfer media for transferring heat to a tubular reactor. The method can include heating a first flowable heat-transfer medium, to provide a heated first flowable heat-transfer medium. The method can include transferring heat from the heated first flowable heat-transfer medium to a second flowable heat-transfer medium, to provide a heated second flowable heat-transfer medium. The method can also include transferring heat from the heated second flowable heat-transfer medium to a tubular reactor of a polyamide synthesis system.

Description

Tubular reactor with improved design for nylon synthesis Cross-application for related applications

The present application claims priority to U.S. Provisional Patent Application Serial No. 61/818,331, filed on Jan. 1, 2013, the disclosure of which is hereby incorporated by reference.

Polyamide has suitable properties such as extreme durability and strength that make it suitable for use in a variety of environments. Polyamines such as nylon, aromatic guanidine polyamines and poly(aspartate) are commonly used in, for example, carpets, airbags, machine parts, garments, ropes and hoses. Nylon-6,6 (a smooth thermoplastic) is one of the most commonly used polyamines. The long molecular chain and dense structure of nylon-6,6 limits it to high quality nylon fibers which exhibit high mechanical strength, stiffness and stability under heating.

Commercially synthesized polyamines in large-scale production facilities. For example, nylon-6,6 can be synthesized by subjecting hexamethylenediamine and adipic acid to a condensation reaction, forming a guanamine linkage, and releasing water. In a series of assemblies including autoclaves or reactors, flashers, and finishing machines, the reaction mixture is heated and the water is gradually removed to drive the equilibrium toward the polyamine until the polymer reaches the desired length range. Next, the molten nylon-6,6 is extruded into pellets which can be spun into fibers or processed into other shapes. The entire production facility requires a large amount of heating to allow the condensation reaction to occur and remove water from the reaction mixture. Typically, the central heating facility heats a single charge filled with volatile heat transfer media. The thermal circuit vaporizes the medium, which is then circulated throughout the apparatus to various components that require heating, including the reactor.

One type of reactor for polyamine synthesis is a tubular reactor. When the tubular reactor heats the reaction mixture, vaporized water (e.g., steam) is produced. The tubular reactor at least partially separates the vapor from the reaction mixture to remove water from the reaction mixture and drive the equilibrium toward the polyamine. When the tubular reactor heats the reaction mixture, rapid thermal changes can occur in the reaction mixture, which is associated with undesirable by-product formation that can contaminate the polyamine product. Rapid thermal changes can also cause gel formation, which can build up and eventually block various components of the system, requiring downtime and cleaning of the reactor and other components, as well as contamination of the polyamide product and negatively affecting properties such as filament strength. When steam is formed in a tubular reactor, it increases the pressure in the reactor and forms a mixture of steam and reaction mixture. The increased pressure allows the vapor and reaction mixture to travel along the tubular reactor at high speed, thereby making the temperature of the reaction mixture difficult to control and complicating the separation of the vapor from the reaction mixture. The high velocity of the vapor and reaction mixture in the reactor allows the reaction mixture to be aerosolized, thereby causing the reaction mixture and the polyamide gel to block the vapor vent, requiring frequent reactor shutdowns for cleaning.

In polyamine synthesis, there are safety risks associated with the use of large amounts of volatile materials as heat transfer media, including fire, combustion and health risks, and there are several components associated with heating circuit heating devices that use a single device. The problem of reduced efficiency and convenience.

This creation provides a method of making polyamines. The method can include heating the first flowable heat transfer medium to provide a heated first flowable heat transfer medium. The method can include transferring heat from the heated first flowable heat transfer medium to the second flowable heat transfer medium to provide a heated second flowable heat transfer medium. The method can also include transferring heat from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system.

This creation provides a method of making nylon-6,6. The method can include heating a first flowable heat transfer medium comprising terphenyl to provide a heated first flowable heat transfer medium. The method can include transferring heat from the first flowable heat transfer medium comprising diphenyl ether and biphenyl to the second flowable heat transfer medium to provide a heated second flowable heat transfer medium and using the first Flowable heat transfer medium. The first flowable heat transfer medium, the heated first flowable heat transfer medium, and the first flowable heat transfer medium used as the first flowable heat transfer medium can be disposed in the primary heating circuit. The first flowable heat transfer medium, the heated first flowable heat transfer during heating of the first flowable heat transfer medium and the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The medium and the used first flowable heat transfer medium can be a substantially liquid phase. The heat transferred to the first flowable heat transfer medium and the heat transferred by the first flowable heat transfer medium can include substantially all of the sensible heat. During the transfer of heat from the first flowable heat transfer medium to the second flowable heat transfer medium, the second flowable heat transfer medium can be substantially completely vaporized. The method can include recycling the first flowable heat transfer medium to a state in which the first flowable heat transfer medium is heated. The method can also include transferring heat from the heated second flowable heat transfer medium to the tubular reactor of the nylon-6,6 synthesis system. The second flowable heat transfer medium and the heated second flowable heat transfer medium can be disposed in the second heating circuit. The second flowable heat transfer medium and the used second flowable heat transfer medium can be substantially liquid phase. The heated second flowable heat transfer medium can be a substantially liquid phase. The heat transferred to the second flowable heat transfer medium and the heat transferred by the second flowable heat transfer medium may include about 70-100% latent heat and about 0-30% sensible heat including heat of vaporization. The method can also include controlling the pressure of the second heat transfer loop to control the saturation temperature of the second flowable heat transfer medium, wherein controlling the saturation temperature controls the temperature of the tubular reactor of the polyamine synthesis system. The method can also include recycling the used second flowable heat transfer medium back to the state of heat transfer from the heated first flowable heat transfer medium. The tubular reactor can have a length of from about 75 to about 125 meters, an inner diameter of from about 25 centimeters to about 60 centimeters, and a length/diameter (L/D) of from about 100 to about 500. The tubular reactor can include from about 10 to about 25 discharge ports along its length.

This creation provides a method of making polyamines. The method can include heating the first The flowable heat transfer medium provides a heated first flowable heat transfer medium. The method can include transferring heat from the heated first flowable heat transfer medium to the second flowable heat transfer medium to provide a heated second flowable heat transfer medium. The method can include transferring heat from the heated second flowable heat transfer medium to a tubular reactor of a polyamine synthesis system. The tubular reactor can have a length of from about 75 to about 125 meters, an inner diameter of from about 25 centimeters to about 60 centimeters, and a length/diameter (L/D) of from about 100 to about 500. The tubular reactor can include from about 10 to about 25 discharge ports along its length.

This creation provides a system for making polyamines. The system can include a heater configured to heat the first flowable heat transfer medium to provide a heated first flowable heat transfer medium. The system can include a first heat exchanger configured to transfer heat from the heated first flowable heat transfer medium to provide a heated second flowable heat transfer medium. The system can also include a second heat exchanger configured to transfer heat from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system.

This creation provides a means of making polyamine. The apparatus can include a heater configured to heat the first flowable heat transfer medium to provide a heated first flowable heat transfer medium. The system can include a first heat exchanger configured to transfer heat from the heated first flowable heat transfer medium to provide a heated second flowable heat transfer medium. The system can also include a second heat exchanger configured to transfer heat from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system.

This creation provides a device for making nylon-6,6. The apparatus can include a heater configured to heat the first flowable heat transfer medium comprising biphenyl to provide a heated first flowable heat transfer medium. The apparatus can include a first heat exchanger configured to transfer heat from the heated first flowable heat transfer medium to a second flowable heat transfer medium comprising diphenyl ether and biphenyl to provide heated The second flowable heat transfer medium and the used first flowable heat transfer medium circulate the used first flowable heat transfer medium back to the first heat exchanger. a first flowable heat transfer medium, a heated first flowable heat transfer medium, and a first flowable heat transfer for use The medium can be placed in a primary heating loop. The first flowable heat transfer medium, the heated first flowable heat transfer during heating of the first flowable heat transfer medium and the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The medium and the used first flowable heat transfer medium can be a substantially liquid phase. The heat transferred to the first flowable heat transfer medium and the heat transferred by the first flowable heat transfer medium can include substantially all of the sensible heat. Additionally, the second flowable heat transfer medium can be substantially completely vaporized during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium. The apparatus can include a second heat exchanger configured to transfer heat from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system to provide a used second flowable heat transfer medium And the used second flowable heat transfer medium is circulated back to the state of heat transfer by the heated first flowable heat transfer medium. The second flowable heat transfer medium and the heated second flowable heat transfer medium can be disposed in the second heating circuit, the second heating circuit configured to control the pressure of the second heat transfer loop to control the second flowable The saturation temperature of the heat transfer medium. Controlling the saturation temperature controls the temperature of the tubular reactor of the polyamine synthesis system. The second flowable heat transfer medium and the used second flowable heat transfer medium can be substantially liquid phase. The heated second flowable heat transfer medium can be a substantially liquid phase. Additionally, the heat transferred to the second flowable heat transfer medium and the heat transferred by the second flowable heat transfer medium may comprise about 70-100% latent heat and about 0-30% sensible heat, the latent heat comprising heat of vaporization. The tubular reactor can have a length of from about 75 to about 125 meters, an inner diameter of from about 25 centimeters to about 60 centimeters, and a length/diameter (L/D) of from about 100 to about 500. The tubular reactor can include from about 10 to about 25 discharge ports along its length.

This creation provides advantages over other methods, systems, and devices for making polyamines, at least some of which are unexpected. If the heating circuit containing a volatile (eg gas) heat transfer medium has a leak point, the leaked material can diffuse to the entire space around the leak point. If the volatile heat transfer medium is flammable, the leak may cause an explosion or fire hazard in the entire space around the leak. In addition, vaporizing the heat transfer medium can make the safety risk far beyond the leak point. If a leak occurs to bring the polymer material into the primary heating circuit, it is used to heat the primary heating back. The formation of coke in the furnace of the road can create a significant risk of fire. A heating circuit containing a non-volatile heat transfer medium (eg, a liquid) can be safer than a heating circuit containing a volatile heat transfer medium. If a leak occurs, the non-volatile material around the leak typically moves to the floor, thereby primarily limiting any ignition and safety risks near the leak and below the leak, and is more volatile than volatile materials. Low explosion risk. If a leak occurs to cause the polymer material to enter the primary heating circuit, the risk of fire from the coke tube in the heater can be significantly less.

A single loop of non-volatile material or a secondary heating loop having a non-volatile material therein can undergo local high temperatures due to the use of sensible heat to transfer heat from the heating loop to the tubular reactor, thereby making it difficult to control the heating of the tubular reactor . Disadvantages associated with the use of non-volatile materials in the heating circuit used to heat the tubular reactor can be avoided by using various embodiments of the present invention: one or more secondary heating circuits (each for heating one or more The use of volatile materials in the assembly, including at least one tubular reactor (for example, at the temperature and pressure used, substantially vaporizes the material when heated and concentrates after cooling), while using a non-volatile heat transfer medium (For example, at the temperature and pressure used, the material remains substantially liquid when heated and after cooling) a one-stage heating circuit to heat the secondary heating circuit. The secondary circuit can be used to heat the tubular reactor and any other components that are optionally present by primarily using latent heat (eg, heat of vaporization) to heat the component. It is easier to control the temperature while avoiding the use of large amounts of volatile materials and avoiding the use of a single heating circuit. Heat all components.

A one-stage loop of a low volatility heat transfer medium that heats the secondary loop of the highly volatile heat transfer medium used to heat the tubular reactor can readily determine the point of leak in the heating loop for the tubular reactor. For example, if a leak occurs in a single heating circuit with vaporized heat transfer material in a number of components (including tubular reactors) surrounding the heating device, the entire circuit must be shut down to repair or extinguish the leak. It is inconvenient and expensive to leak a supply of fire that causes most of the equipment to go offline. However, by containing vaporized heat transfer material in the secondary loop specific to the tubular reactor, the leak point in the secondary loop Only the circuit needs to be repaired, and the rest of the equipment can continue to operate normally. In various instances, the safety risks associated with the use of volatile heat transfer materials are reduced by the use of non-volatile heat transfer media in the primary circuit and by the avoidance of the use of large amounts of volatile flammable heat transfer media. For example, the risk of a leak in a large primary circuit containing a liquid phase heat transfer material may be less severe than a leak in a large loop containing a vaporized heat transfer material.

The use of a single loop of heat transfer material limits the temperature of the materials available for heat transfer to a narrow temperature range. The use of a secondary loop having a volatile heat transfer medium therein for the tubular reactor can make it easy to control the temperature of the heat transfer medium. A primary loop can be used to vaporize the volatile material in the secondary loop, which can be condensed to transfer heat to the tubular reactor. The pressure in the secondary circuit can be adjusted to control the saturation temperature of the heat transfer medium, thereby accurately controlling the temperature of vaporization and condensation of the volatile heat transfer medium in the secondary circuit, thereby interacting with other methods, systems and devices for producing polyamine The temperature of the device components is controlled to a greater extent. When multiple secondary circuits are used, each contains a volatile heat transfer medium, which can easily control the saturation temperature of the heat transfer medium in each secondary circuit.

The use of a single loop with a volatile heat transfer material (vapor/gas phase) may initially involve heating the heat transfer material to a temperature well beyond that of the various components of the apparatus. This can cause the heat transfer material to overheat (eg, for a given pressure to reach a temperature above the saturation temperature). If strict temperature control is required, additional complexity is required to remove the overheating to achieve temperature uniformity. In various embodiments, the secondary loop may allow for the use of heat transfer materials at or near saturation temperatures in the secondary loop, thereby achieving high temperature uniformity under less complex equipment. In various embodiments, it may be more efficient to use saturated steam relative to superheated steam for heat transfer. If the vapor is significantly overheated, the vapor is first cooled to saturation temperature before condensation occurs. The heat transfer coefficient of superheated steam is lower than that of condensed vapor. In various embodiments, a heat transfer material in the form of a saturated vapor that uses less superheat than other methods or devices allows for a given surface area to transfer more heat, or allows a smaller surface area to achieve equal heat transfer. In various embodiments, such as in a process that requires high heat, a low wave is used in the primary heating loop. The use of condensed vapor in the secondary fluid and in the secondary circuit reduces the heat transfer area (process vessel size).

The tubular reactor can heat the polyamine reaction mixture too quickly, which can result in the formation of undesirable by-products that can contaminate the desired polyamine product. Rapid thermal changes can also cause gel formation, which can build up and eventually block various components of the system, requiring downtime and cleaning of the reactor and other components. Rapid thermal changes can produce large diamine losses in the steam produced. Rapid thermal changes can increase the aerosolization of the reaction mixture, thereby causing the reaction mixture and the polyamine gel to block the vapor vent, requiring the reactor to be shut down more frequently for cleaning. The present invention can provide a tubular reactor that can be longer in length, have at least one of smaller diameters, or have a greater length/diameter ratio than other tubular reactors, thereby making the reaction mixture slower and Gently heat to the target temperature. The present work can provide a tubular reactor having a larger surface area to volume ratio than other tubular reactors, thereby allowing the reaction mixture to be heated more gently. Thus, the present work can provide a tubular reactor that produces less undesirable by-products during polyamine synthesis, less gel formation and accumulation, requires less frequent shutdown and cleaning, and is in the reaction mixture. Less loss of diamine.

The tubular reactor can have a diameter that increases from the entry end to the exit end of the reactor. If the expansion rate along the length of the length is too fast, the reactor can cool the polyamine reaction mixture too quickly, causing the reaction mixture to gel and solidify, whereby the reactor may need to be shut down for cleaning more frequently. The present invention can provide a tubular reactor with a small expansion rate that may be sufficient to reduce or minimize gelation and solidification of the reaction mixture, thus requiring less frequent shutdowns than other tubular reactors having greater expansion rates. And clean. The present invention can provide a tubular reactor having a pressure sufficient to reduce the pressure from the inlet end to the exit end of the reactor as appropriate from the reaction mixture, as compared to other tubular reactors having a lower expansion rate or no expansion ratio. More efficient removal of water expansion rate.

The high speed of the steam and polyamine reaction mixture in the tubular reactor allows the reaction to mix The aerosol is aerosolized, thereby causing the reaction mixture and the polyamide gel to block the steam vent, requiring frequent reactor shutdowns for cleaning. The high velocity in the tubular reactor can also make it difficult to control the temperature of the reaction mixture. The present invention can provide a tubular reactor having a discharge port that can be more or better distributed along the length than other tubular reactors, such that the acceleration of the reaction mixture via steam generation can be reduced or minimized. Reduce aerosolization and simplify temperature control of the reaction mixture. The present work can provide a method of injecting a solvent, such as water, into a discharge line that reduces or minimizes the formation or accumulation of gel or other materials in the discharge line. Reduced or minimized aerosolization or water flooding can provide a tubular reactor that requires less frequent shutdown and cleaning than other tubular reactors.

In various embodiments, the tubular reactor can have a plurality of discharge ports and a space between the discharge ports, thereby providing a larger proportion of the annular flow compared to other tubular reactors to create between the reaction mixture and the reactor. Higher heat transfer area compared to other tubular reactor designs. For example, some embodiments have a larger spacing between the discharge ports than other tubular reactors to provide a better annular flow, the other tubular reactors having less space and experiencing air bubbles along the top of the reactor or The reaction mixture along the bottom of the reactor forms a flow pattern that is approximately semi-cylindrical. For example, some embodiments have a smaller spacing between the discharge ports than other tubular reactors to provide a preferred annular flow, the other tubular reactors having a larger space and undergoing partial flashing and embolization of the reaction mixture Flow state.

1‧‧‧ tubular reactor

2‧‧‧ entrance

3‧‧‧Export

4‧‧‧ Straight section

5‧‧‧Bend section

6‧‧‧Export

10‧‧‧Systems or devices for the manufacture of polyamines

15‧‧‧heater

20‧‧‧First flowable heat transfer medium

21‧‧‧Systems or devices for the manufacture of polyamines

25‧‧‧First heating circuit

30‧‧‧The first flowable heat transfer medium heated

35‧‧‧First heat exchanger

36‧‧‧ Third heat exchanger

40‧‧‧Second flowable heat transfer medium

41‧‧‧ Third flowable heat transfer medium

45‧‧‧Secondary heating circuit

46‧‧‧Three-stage heating circuit

50‧‧‧heated second flowable heat transfer medium

51‧‧‧heated third flowable heat transfer medium

55‧‧‧second heat exchanger

56‧‧‧fourth heat exchanger

The drawings, which are not necessarily to scale, are in the

Figure 1 illustrates a tubular reactor in accordance with various embodiments.

2 illustrates a system or apparatus in accordance with various embodiments.

FIG. 3 illustrates a system or apparatus in accordance with various embodiments.

Reference is now made in detail to the preferred embodiments, It is to be understood that the scope of the invention is not limited by the scope of the invention.

Values expressed in a range format are to be interpreted in a flexible manner to include not only the numerical value of the scope of the invention, but also all the individual values or sub-ranges that are included in the scope of the invention. For example, the range of "about 0.1% to about 5%" or "about 0.1% to 5%" should be interpreted to include not only about 0.1% to about 5%, but also individual values in the range shown (for example, 1%). , 2%, 3%, and 4%) and sub-ranges (eg, 0.1% to 0.5%, 1.1% to 2.2%, 3.3% to 4.4%). Unless otherwise indicated, the statement "about X to Y" has the same meaning as "about X to about Y". Similarly, "about X, Y or about Z" has the same meaning as "about X, about Y or about Z" unless otherwise indicated.

Unless the context clearly dictates otherwise, the term "a" or "the" is used in this document to include one or more. Unless otherwise stated, the use of the term "or" means non-exclusive "or". In addition, it should be understood that the phraseology or terminology used herein is not intended to be a Any use of chapter headings is intended to aid in reading the literature and should not be construed as limiting; information relating to chapter headings may exist within a particular section or outside a particular section. In addition, all publications, patents, and patent documents relating to this document are hereby incorporated by reference in their entirety in their entirety in their entirety in their entirety. In the event of inconsistency between this document and the documents incorporated by reference, the use incorporation in the reference should be considered a supplement to the use of this document; for irreconcilable contradictions, the use in this document is the Lord.

In the fabrication methods described herein, the various steps can be carried out in any order, without departing from the principles of the present invention. In addition, the specified steps may be performed simultaneously unless the explicit technical solution wording states that the specified steps are performed separately. For example, the claimed step of performing X and the claimed step of performing Y The steps can be performed simultaneously in a single operation, and the resulting method will fall within the scope of the claimed method.

The term "about" as used herein may allow a value or range of variability, such as within 10%, within 5%, or within 1% of the stated value of the stated value or range.

As used herein, the term "substantially" means most or most, as at least about 50%, 60%, 70%, 80%, 90%, 95%, 96%, 97%, 98%, 99%, 99.5%, 99.9%, 99.99% or at least about 99.999% or 99.999% or more.

As used herein, the term "solvent" refers to a liquid that dissolves a solid, liquid or gas. Non-limiting examples of solvents are polyoxo, organic compounds, water, alcohols, ionic liquids, and supercritical fluids.

As used herein, the term "standard temperature and pressure" means 0 ° C and 100 KPa.

As used herein, the term "polymer" can include a copolymer.

As used herein, the term "heat exchanger" means a device that transfers heat from one medium to another. The media can be separated by solid walls. Examples of heat exchangers include shell and tube heat exchangers, plate heat exchangers, plate and shell heat exchangers, insulated wheel heat exchangers, plate fin heat exchangers, pad heat exchangers, fluid heat exchangers, Waste heat recovery unit, dynamic scraped surface heat exchanger and phase change heat exchanger.

As used herein, the term "sensible heat" refers to the heat exchanged by a host or thermodynamic system, wherein the exchange effect is substantially a temperature change of the host or system and a small or even no phase change.

As used herein, the term "latent heat" refers to the heat exchanged by a host or thermodynamic system, wherein the exchange effect is essentially a phase change of the host or system with little or no temperature change.

As used herein, the term "relative viscosity" (RV) refers to the ratio of solution to solvent viscosity as measured by capillary viscosity at 25 °C. In one example, the RV obtained by ASTM D789-06 is the viscosity (in centipoise) of a solution of 8.4 wt% polyamine in 90% formic acid (90 wt% formic acid and 10 wt% water) at 25 °C. ) with 90% formic acid viscosity at 25 ° C alone The ratio (in centipoise).

As used herein, the term "saturation temperature" refers to the temperature at which a liquid boils to its gas phase at a particular pressure (eg, at a temperature at which it is saturated) and the temperature at which the vapor begins to condense into its liquid phase. At the saturation temperature at a particular pressure of the material, the material will condense as the temperature decreases or the pressure increases. At the saturation temperature at a particular pressure of the material, as the temperature increases or the pressure decreases, the material will boil into its gas phase.

The present invention relates to a method, system and apparatus for the manufacture of polyamines having at least two heat transfer media that transfer heat to a tubular reactor. The polyamine can be any suitable polyamine, such as nylon 6, nylon 7, nylon 11, nylon 12, nylon 6,6, nylon 6,9; nylon 6,10, nylon 6,12, partially aromatic polyfluorene An amine (such as high temperature nylon) or a copolymer thereof.

The method of making polyamine.

The method can include heating the first flowable heat transfer medium to provide a heated first flowable heat transfer medium. Heating can be carried out in any suitable manner. Heating can be carried out in a heat exchanger, such as any suitable heat exchanger. The first flowable heat transfer medium can be located in the heating circuit. The first flowable heat transfer medium can be heated in a power chamber or central heating zone in the facility and can be used to transfer heat from the primary heating loop to the secondary heating loop throughout the facility, and then reheated back into the power chamber. A secondary heating circuit can be used to heat one or more tubular reactors in the facility. The first flowable heat transfer medium can be non-volatile such that the first flowable heat transfer medium can be substantially in a liquid phase before and after heating.

The primary heating circuit and the one or more secondary heating circuits can have any suitable volume relative to each other. The volume of the primary heating circuit can be greater than the secondary heating circuit. The primary heating circuit can have substantially the same volume or a smaller volume than the secondary heating circuit. The primary heating circuit may have a volume of from about 0.0001% to 1,000,000% of the secondary heating circuit, or from about 100% to 1,000,000%, or about 0.0001% or 0.0001% or less, or about 0.001%, 0.01%, 0.1 of the secondary heating circuit. %, 1%, 5%, 10%, 25%, 50%, 75%, 100%, 125%, 150%, 175%, 200%, 300%, 400%, 500%, 750%, 1000%, 1500%, 2000%, 3000%, 4000%, 5000%, 10,000%, 20,000%, 50,000%, 100,000%, about 500,000% or about 1,000,000% or more than 1,000,000% by volume. The first flowable heat transfer medium and the heated first flowable heat transfer medium and the second flowable heat transfer medium and the heated second flowable heat transfer medium can have any suitable mass ratio. For example, the ratio of the mass combination of the first flowable heat transfer medium and the heated first flowable heat transfer medium to the mass of the second flowable heat transfer medium and the heated second flowable heat transfer medium may be From about 0.0000001:1 to about 10,000,000:1, about 100:1 to about 100:1, about 0.0000001:1 or 0.0000001:1 or less, or about 0.0001:1, 0.001:1, 0.01:1, 0.1:1, 1 : 1, 5: 1, 10: 1, 25: 1, 50: 1, 75: 1, 100: 1, 125: 1, 150: 1, 175: 1, 200: 1, 300: 1, 400: 1 , 500:1, 750:1, 1000:1, 1500:1, 2000:1, 3000:1, 4000:1, 5000:1, 10,000:1, 20,000:1, 50,000:1,100,000:1,500,000 : 1, about 1,000,000: 1 or about 10,000,000: 1 or 10,000,000: 1 or more.

The method can include transferring heat from the heated first flowable heat transfer medium to the second flowable heat transfer medium to provide a heated second flowable heat transfer medium. Heating can be carried out in any suitable manner. Heating can be carried out in a heat exchanger, such as any suitable heat exchanger. The second flowable heat transfer medium can be sufficiently volatile such that it can be heated to a substantially gaseous phase by the first flowable heat transfer medium and to the tubular reactor by the heated second flowable heat transfer medium It can be condensed into a substantially liquid phase during heat transfer.

The first flowable heat transfer medium can remain liquid as it is heated and heat transferred, while the second flowable heat transfer medium can vaporize when heated and condense when heat is transferred therefrom. The first flowable heat transfer medium may have a lower vapor pressure than the second flowable heat transfer medium at standard temperature and pressure; or the first flowable heat transfer medium may have a second flowable heat transfer medium Compared to the vapor pressure of the delivery. The pressure of the second flowable heat transfer medium can be controlled to vaporize and condense at the desired temperature. Because the first flowable heat transfer medium can remain liquid after heating, and the second flowable heat transfer medium can be substantially vaporized after heating, and is heated The heated second flowable heat transfer medium can have a higher vapor pressure than the first flowable heat transfer medium.

Both the first flowable heat transfer medium and the second flowable heat transfer medium may be flammable organic materials, or both may include flammable organic components. Vaporized and high vapor pressure flammable organic materials are often associated with greater ignition and combustion risks than liquid flammable organic compounds with lower vapor pressures. The heated second flowable heat transfer medium can be at least one of more flammable and more flammable than the heated first flowable heat transfer medium.

The method can also include transferring heat from the heated second flowable heat transfer medium to the tubular reactor. Heat transfer can be carried out in any suitable manner. The heat transfer can be carried out in a heat exchanger, such as any suitable heat exchanger. Heat may be transferred to the one or more tubular reactors by the heated second flowable heat transfer medium and, as appropriate, to one or more other equipment components, such as preheaters, evaporators, polymerization reactors, flashers, At least one of a finishing machine and an autoclave. The preheater can be any suitable preheater and can be coupled to any suitable component of the facility, such as a preheater for at least one of an evaporator, a polymerization reactor, a flasher, a finishing machine, and an autoclave. The temperature of the individual components can be brought to any suitable temperature or temperature range by the heated second flowable heat transfer medium. For example, sufficient heat can be transferred to the evaporator to raise the temperature of the reaction mixture therein to any suitable temperature, such as about 100-230 ° C, or 100-150 ° C, or about 100 ° C or less, or about Temperatures of 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C or about 230 ° C or more. For example, sufficient heat can be transferred to the reactor to raise the temperature of the reaction mixture therein to any suitable temperature, such as about 150-300 ° C, or about 200-250 ° C, or about 215-245 ° C, or about 215. °C or 150 ° C or less, or about 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 215 ° C, 220 ° C, 225 ° C, 230 ° C, 235 ° C, 240 ° C, 245 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 ° C or about 300 ° C or more than 300 ° C temperature. For example, sufficient heat can be transferred to the flasher to raise the temperature of the reaction mixture therein to any suitable Temperature, such as about 150-400 ° C, or about 275-350 ° C, or about 215-310 ° C, or about 200 ° C or less, or about 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 Temperatures of °C, 265°C, 270°C, 275°C, 280°C, 285°C, 290°C, 295°C, 300°C, 305°C, 310°C, 320°C, 330°C, 340°C or about 350°C or above 350°C . For example, sufficient heat can be delivered to the finishing machine to raise the temperature of the reaction mixture therein to any suitable temperature, such as about 150-400 ° C, or about 250-350 ° C, or about 250-310 ° C, or about 200 ° C or less, or about 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 265 ° C, 270 ° C, 275 ° C, 280 ° C, 285 ° C, 290 ° C, 295 ° C, 300 ° C 305 ° C, 310 ° C, 320 ° C, 330 ° C, 340 ° C or a temperature of about 350 ° C or above.

Transferring heat from the heated second flowable heat transfer medium to the tubular reactor can include maintaining the temperature of the tubular reactor at any suitable temperature, such as from about 100 ° C to about 400 ° C, from 150 ° C to 350 ° C, from 150 ° C to 250 ° °C, 250 ° C to 350 ° C, 200 ° C to 300 ° C, or about 210 ° C to 260 ° C, or about 218 ° C to about 250 ° C, or about 100 ° C, 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C , 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 205 ° C, 210 ° C, 215 ° C, 220 ° C, 225 ° C, 230 ° C, 235 ° C, 240 ° C, 245 ° C, 250 ° C, 255 ° C, 260 °C, 265°C, 270°C, 280°C, 290°C, 300°C, 310°C, 320°C, 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C or about 400°C or 400°C the above. Transferring heat from the heated second flowable heat transfer medium to at least one component of the polyamine synthesis system can include maintaining the temperature of the polyamidamine mixture in the reactor at any suitable temperature, such as from about 210 ° C to 260 ° C, 218 ° C to about 250 ° C, or about 100 ° C or less, or about 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 205 ° C , 210 ° C, 215 ° C, 220 ° C, 225 ° C, 230 ° C, 235 ° C, 240 ° C, 245 ° C, 250 ° C, 255 ° C, 260 ° C, 265 ° C, 270 ° C, 280 ° C, 290 ° C, 300 ° C, 310 °C, 320°C, 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C Or about 400 ° C or above.

Although heating of the unit operations has been described, one skilled in the art will appreciate that one of the one or more unit operations can be cooled using the general methods described herein.

Tubular reactor

The tubular reactor can be any suitable tubular reactor that can heat the polyamine reaction mixture. The tubular reactor can have any suitable shape and design. The tubular reactor can include a cylindrical tube having a jacket thereon that transfers heat to the reactor. The heat transfer fluid can flow through the reactor jacket.

An illustration of a suitable tubular reactor 1 is shown in FIG. The tubular reactor 1 comprises an inlet 2 and an outlet 3. The tubular reactor 1 comprises a straight section 4 and a curved section 5. The tubular reactor comprises a discharge opening 6.

The tubular reactor can have any suitable length, such as the length between the inlet and the outlet along the straight and curved sections. The tubular reactor can have from about 50 to 300 meters, or from about 75 to 125 meters, or from about 90 to 110 meters, or from about 50 meters or less to 50 meters, or about 60 meters, 70 meters, 80 degrees. Metric, 85 meters, 90 meters, 95 meters, 100 meters, 105 meters, 110 meters, 115 meters, 120 meters, 130 meters, 140 meters, 150 meters, 160 meters , 170 meters, 180 meters, 190 meters, 200 meters, 225 meters, 250 meters, 275 meters or about 300 meters or more than 300 meters in length.

The tubular reactor can have any suitable inner diameter, such as the inner diameter of the straight section and the curved section. The inner diameter may vary from one end of the reactor to the other, or the inner diameter may be constant. For example, the inner diameter from the entry end of the tubular reactor to the exit end of the tubular reactor is expandable. The tubular reactor can have from about 10 cm to 80 cm, or from about 25 cm to about 60 cm, or from about 35 cm to 50 cm, or from about 10 cm or less, or from about 15 cm, 20 cm, 25 cm, 30 cm, 35 cm, 36 cm, 37 cm, 38 cm, 39 cm, Inner diameters of 40 cm, 41 cm, 42 cm, 43 cm, 44 cm, 45 cm, 46 cm, 47 cm, 48 cm, 49 cm, 50 cm, 55 cm, 60 cm, 65 cm, 70 cm, 75 cm or about 80 cm or more. If the tubular reactor comprises a jacket, the jacket may have any suitable outer diameter, such as super An inner diameter of 1 to 50 cm, or an inner diameter of about 1 to 25 cm, or about 1 cm or less, or an inner diameter of about 2 cm, 4 cm, 6 cm, 8 cm, 10 cm, 12 cm, 14 cm, 16 cm, 18 cm, 20 cm, 22 cm, 24, 26, 28, 30, 32, 34, 36, 38, 40, 42, 44, 46, 48, or about 50 or more.

The tubular reactor can have a constant inner diameter or be expandable from the entry end to the exit end of the reactor, such as linear expansion or non-linear expansion. The diameter can be expanded sufficiently to maintain a substantially constant pressure from the inlet end to the exit end of the reactor when the reactor is used. The diameter is expandable such that the pressure from the inlet end to the exit end is reduced when the reactor is used. The expansion rate of the tubular reactor may be sufficient to allow the heat applied to the reaction mixture, the amount of water removed by vaporization and removal from the reaction mixture, and the combination of pressures of the reaction mixture at a predetermined location along the length to help maintain the flow of the reaction mixture. The exit end of the reactor reduces or minimizes the generation or accumulation of gel or other impurities. The inner diameter of the reactor may be extended by about 2.5 cm for every length of from about 6.25 m to about 750 m, about 2.5 cm for every 22.5 m to about 550 m length, and about 2.5 cm, or about every 22.5 m to about 110 m length. 6m or less, or about 8m, 10m, 15m, 20m, 25m, 30m, 35m, 40m, 45m, 50m, 55m, 60m, 65m, 70m, 75m, 80m, 85m, 90m, 95m, 100m, 105m, 110, 120, 125, 150, 175, 200, 225, 250, 275, 300, 325, 350, 375, 400, 425, 450, 475, 500, 550, 550, 600, 650, 700, or It can be expanded by about 2.5cm.

The tubular reactor can have any suitable length/diameter (L/D, such as length divided by average diameter). For example, the length/diameter (L/D) of the tubular reactor can be from about 50 to 2500, or from about 100 to 500, or from about 230 to 270, from about 50 or less, or from about 75, 100, 125, 150. , 175, 200, 210, 220, 230, 235, 240, 245, 250, 255, 260, 265, 270, 280, 290, 300, 400, 500, 600, 700, 800, 900, 1000, 1250, 1500, 1750, 2000, 2250 or about 2500 or more.

The tubular reactor can include a discharge port along its length. The tubular reactor can include any suitable amount and type of discharge port so that steam can be released from the discharge port. The tubular reactor can include any suitable amount of discharge ports along its length. For example, the tubular reactor can have from about 5 to 50 discharge ports, or from about 10 to 25 discharge ports along its length, or about 5 or less discharge ports along its length, or about 6, 7, 8 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, 24, 25, 30, 35, about 45 discharges.

The discharge port may be present in the tubular reactor at any suitable average distance from adjacent discharge ports. For example, the tubular reactor is along the length of the tubular reactor from about 2 meters to about 15 meters, or from about 3 meters to about 9 meters, or has an average of about 5 to about 8 meters along the length. Can be about 1 discharge port, or about 2 meters or less along the length of the tubular reactor, or about 3 meters, 4 meters, 5 meters, 6 meters, 7 meters, 8 meters 9 outlets of 9 meters, 10 meters, 11 meters, 12 meters, 13 meters, 14 meters or about 15 meters or more than 15 meters.

The tubular reactor can have any suitable average spacing between the discharge ports along its length. For example, the tubular reactor can have an average spacing of between about 2 meters and about 15 meters, or between about 3 meters to about 9 meters, or about 5 to about 5 meters between the discharge ports along the length of the tubular reactor. About 8 meters, or about 2 meters or less along the length, or about 3 meters, 4 meters, 5 meters, 6 meters, 7 meters, 8 meters, 9 meters, 10 meters A distance of 11 feet, 11 meters, 12 meters, 13 meters, 14 meters, or about 15 meters or more.

The tubular reactor can have a quantity and a distribution of outlets such that the velocity of the vapor within the tubular reactor does not exceed any suitable maximum. For example, the number and distribution of the discharge ports may be sufficient to provide a steam velocity in the tubular reactor of no more than about 0.5 m/s to about 400 m/s, 1 to 200 m/s, 2 to 100 m/s, 4 to 50 m/s. Or about 0.5 m/s or less, or about 1 m/s, 2 m/s, 3 m/s, 4 m/s, 5 m/s, 15 m/s, 10 m/s, 20 m/s, 25 m/s , 30m/s, 35m/s, 40m/s, 45m/s, 50m/s, 55m/s, 60m/s, 65 m/s, 70 m/s, 75 m/s, 80 m/s, 85 m/s, 90 m/s, 95 m/s, 100 m/s, 125 m/s, 150 m/s, 175 m/s, 200 m/s, 250 m/ s, 300 m/s or about 400 m/s or more.

The tubular reactor can flow through a polymeric material having any suitable flow rate. For example, the flow rate can be from 1 L/min to about 1,000,000 L/min, or from about 10 L/min to about 100,000 L/min, or about 1 L/min or less, 10 L/min, 20 L/min, 30 L/ Min, 40L/min, 50L/min, 60L/min, 70L/min, 80L/min, 90L/min, 100L/min, 125L/min, 150L/min, 175L/min, 200L/min, 225L/min, 250L/min, 275L/min, 300L/min, 350L/min, 400L/min, 450L/min, 500L/min, 600L/min, 700L/min, 800L/min, 900L/min, 1,000L/min, 2,500 L/min, 5,000 L/min, 10,000 L/min, 50,000 L/min, 100,000 L/min, 500,000 L/min or about 1,000,000 L/min or more than 1,000,000 L/min. The polymerization system comprising a tubular reactor can produce a polymer at any suitable rate, such as from about 1 L/min to about 1,000,000 L/min, or from about 10 L/min to about 100,000 L/min, or about 1 L/min or less. 10L/min, 20L/min, 30L/min, 40L/min, 50L/min, 60L/min, 70L/min, 80L/min, 90L/min, 100L/min, 125L/min, 150L/min, 175L/ Min, 200L/min, 225L/min, 250L/min, 275L/min, 300L/min, 350L/min, 400L/min, 450L/min, 500L/min, 600L/min, 700L/min, 800L/min, 900 L/min, 1,000 L/min, 2,500 L/min, 5,000 L/min, 10,000 L/min, 50,000 L/min, 100,000 L/min, 500,000 L/min or about 1,000,000 L/min or 1,000,000 L/min or more .

The tubular reactor can have a quantity and a distribution of outlets such that the tubular reactor has any suitable F factor. The discharge port can be connected to a suitable discharge line. The method can include injecting water into the discharge line. Water can be injected into each of the discharge ports at any suitable rate.

The tubular response of this creation between shutdown and cleaning to remove gel or other contaminants The device can operate any suitable time. For example, the method can be carried out for at least about 1 to 7 years, 2 to 5 years, or about 2.3 to 3 years, or about 3 years without the tubular reactor being cleaned.

The tubular reactor can have any suitable reaction mixture and vapor in a fluid state. For example, a tubular reactor can have primarily an annular flow (eg, most of the liquid is in internal contact with the reactor tube, while gas and vapor travel primarily down the middle of the reactor tube). In some examples, the tubular reactor can have a plug flow (eg, a substantially continuous liquid cylinder in the tube is interspersed with a substantially continuous gas and a vapor cylinder in the tube) and other fluid states (eg, the liquid remains at the bottom of the tube to form an approximation) Semi-cylindrical, while gas and steam remain at the top of the tube). Any suitable combination of annular flow, plug flow, and other flow regimes may be present in the tubular reactor.

In various examples, the reactor can heat the reaction mixture and evaporate water therefrom to push the equilibrium further toward the polyamine product. The reaction mixture can be heated in the reactor to any suitable temperature, such as about 150-400 ° C, or about 250-350 ° C, or about 250-310 ° C, or about 200 ° C or less, or about 210 ° C, 220. °C, 230°C, 240°C, 250°C, 260°C, 265°C, 270°C, 275°C, 280°C, 285°C, 290°C, 295°C, 300°C, 305°C, 310°C, 320°C, 330°C, 340 ° C or about 350 ° C or above. The reaction mixture leaving the reactor may have any suitable weight percentage of water, such as from about 0.0001% to 20% by weight, from 0.001 to 15% by weight, or from about 0.01 to 15% by weight, or from about 0.0001% by weight or 0.0001% by weight, Or about 0.001%, 0.01%, 0.05%, 0.06%, 0.07%, 0.08%, 0.09%, 0.1%, 0.2%, 0.3%, 0.4%, 0.5% by weight, 0.6% by weight, 0.7% by weight, 0.8% by weight, 0.9% by weight, 1.0% by weight, 1.2% by weight, 1.4% by weight, 1.6% by weight, 1.8% by weight, 2% by weight, 3% by weight, 4% by weight, and 5 parts by weight %, 6% by weight, 7% by weight, 8% by weight, 9% by weight, 10% by weight, 11% by weight, 12% by weight, 13% by weight, 14% by weight, 15% by weight, 16% by weight, 17% by weight, 18% by weight, 19% by weight or about 20% by weight or more.

System and device for manufacturing polyamine.

This creation provides a system for making polyamines. The system can be any suitable system that can perform the methods described herein. The system includes a heater. The heater can be any suitable heater. The heater can be configured to heat the first flowable heat transfer medium to provide a heated first flowable heat transfer medium.

The system can include a first heat exchanger. The first heat exchanger can be any suitable heat exchanger. The first heat exchanger can be configured to transfer heat from the heated first flowable heat transfer medium to provide a heated second flowable heat transfer medium.

The system can include a second heat exchanger. The second heat exchanger can be any suitable heat exchanger. The second heat exchanger can be configured to transfer heat from the heated second flowable heat transfer medium to at least one tubular reactor of the polyamine synthesis system.

This creation provides a means of making polyamine. The system can be any suitable device that can perform the methods described herein. The device can include a heater. The heater can be any suitable heater. The heater can be configured to heat the first flowable heat transfer medium to provide a heated first flowable heat transfer medium.

The device can include a first heat exchanger. The first heat exchanger can be any suitable heat exchanger. The first heat exchanger can be configured to transfer heat from the heated first flowable heat transfer medium to provide a heated second flowable heat transfer medium.

The device can include a second heat exchanger. The second heat exchanger can be any suitable heat exchanger. The second heat exchanger can be configured to transfer heat from the heated second flowable heat transfer medium to at least one tubular reactor of the polyamine synthesis system.

Figure 2 illustrates an embodiment of a system or apparatus 10 for making polyamine. The system or device can include a heater 15. The heater heats the first flowable heat transfer medium 20 disposed in the primary heating circuit 25 to provide a heated first flowable heat transfer medium 30. The system or device can include a first heat exchanger 35. The first heat exchanger 35 transfers heat from the heated first flowable heat transfer medium 30 to the second flowable heat transfer medium 40 disposed in the secondary heating circuit 45 to provide a heated second flowable heat transfer Medium 50. Making the first flowable heat transfer medium 20 (for example, The first flowable heat transfer medium is passed back to the heater 15 for reheating. The system or device can include a second heat exchanger 55. The second heat exchanger 55 transfers heat from the heated second flowable heat transfer medium 50 to the tubular reactor in the polyamine synthesis system integrated with the second heat exchanger 55. The second flowable heat transfer medium 40 (e.g., the used second flowable heat transfer medium) is transferred back to the second heat exchanger 35 for reheating. The system or device can deliver the heat transfer medium from one location to another using any suitable means, such as pumping or convection.

Figure 3 illustrates an embodiment of a system or apparatus 21 for making polyamine. The system or device can include a heater 15. The heater 15 heats the first flowable heat transfer medium 20 disposed in the primary heating circuit 25 to provide a heated first flowable heat transfer medium 30. The system or device can include a first heat exchanger 35. The first heat exchanger 35 transfers heat from the heated first flowable heat transfer medium 30 to the second flowable heat transfer medium 40 disposed in the secondary heating circuit 45 to provide a heated second flowable heat transfer Medium 50. The system or device can include a second heat exchanger 55. The second heat exchanger 55 transfers heat from the heated second flowable heat transfer medium 50 to the tubular reactor in the polyamine synthesis system integrated with the second heat exchanger 55. The second flowable heat transfer medium 40 (e.g., the used second flowable heat transfer medium) is transferred back to the second heat exchanger 35 for reheating. The heated first flowable heat transfer medium 30 is passed into the third heat exchanger 36. The third heat exchanger 36 transfers heat from the heated first flowable heat transfer medium 30 to the third flowable heat transfer medium 41 disposed in the tertiary heating circuit 46 to provide a heated third flowable heat transfer Medium 51. The system or apparatus can include a fourth heat exchanger 56. The fourth heat exchanger 56 transfers heat from the heated third flowable heat transfer medium 51 to at least one polyamine containing group of polyamine synthesis systems that are integrated with the fourth heat exchanger 56, the polyamine containing The component is such as a salt strike, an evaporator, a reactor or a flasher. The third flowable heat transfer medium 41 (e.g., the used second flowable heat transfer medium) is passed back to the third heat exchanger 36 for processing. The first flowable heat transfer medium 20 (e.g., the used first flowable heat transfer medium) is transferred back to the heater 15 for reheating.

Although FIG. 3 illustrates an embodiment in which the first heat exchanger 35 and the third heat exchanger 36 are connected in series, The third heat exchanger 36 is caused to receive the heated first flowable heat transfer medium 30 after the heated first flowable heat transfer medium 30 transfers heat to the second flowable heat transfer medium 40, but the present disclosure also covers Parallel configuration of heat exchangers for exchanging heat between primary and secondary heating circuits. For example, in one embodiment, the third heat exchanger 36 may extract the heated first flowable point at a point upstream of the first heating circuit that is returned from the heat exchanger 35 using the first flowable heat transfer medium. The heat transfer medium is such that the third heat exchanger does not extract the first flowable heat transfer medium that has transferred some heat to the second flowable heat transfer medium 40 in the first heat exchanger 35.

The first flowable heat transfer medium.

In the method, system or apparatus, the first flowable heat transfer medium can be any suitable flowable heat transfer medium. The first flowable heat transfer medium can include one or more organic compounds having characteristics that make the first flowable heat transfer medium suitable for use in the methods, systems, and devices described herein. The first heat transfer medium flow can be for example, water, polyethylene glycol, polypropylene glycol, mineral oil, polyethylene oxide silicon oil, ether (diphenyl oxide), biphenyl, THERMINOL ^® brand heat transfer fluid and DOWTHERM ^TM brand At least one of the hot fluids. First heat transfer medium flow may be, for example, THERMINOL ^® brand heat transfer fluid, such as at least one of: THERMINOL ^® VLT (e.g. methylcyclohexane, trimethylpentane), THERMINOL ^® D-12 (e.g. C _{10 -13} alkanes such as isoalkanes), THERMINOL ^® LT (eg diethylbenzene), THERMINOL ^® XP (eg white petroleum mineral oil), THERMINOL ^® 55 (eg C _14-30 alkyl aryl compounds), THERMINOL ^® 59 (eg ethyl diphenylethane, diphenylethane, diethyldiphenylethane, ethylbenzene polymer), THERMINOL ^® 62 (eg diisopropyl biphenyl, triisopropyl biphenyl), THERMINOL ^® VP-3 (eg cyclohexylbenzene, dicyclohexyl), THERMINOL ^® 66 (eg biphenyl (orthotriphenyl, meta-triphenyl, bis-triphenyl), hydrogenated terphenyl, partially hydrogenated bis-tetraphenyl) , partially hydrogenated high carbon polyphenylene), THERMINOL ^® 72 (eg diphenyl ether, terphenyl, biphenyl, phenanthrene), THERMINOL ^® VP-1 (eg diphenyl ether, biphenyl), THERMINOL ^® FF (eg vinylated benzene). The first flowable heat transfer medium may include, for example, trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _14-30 alkyl aryl compound, diethylbenzene, vinylated benzene, cyclohexyl Benzene, C _14-30 alkyl benzene, white petroleum mineral oil, ethyl diphenylethane, diphenylethane, diethyl diphenylethane, diphenyl ether, diphenyl oxide , ethyl benzene polymer, biphenyl, inorganic salt, diisopropyl biphenyl, triisopropyl biphenyl, methyl cyclohexane, bicyclohexane, terphenyl, hydrogenated terphenyl, partial hydrogenation couplet Tetrabenzene, partially hydrogenated high carbon polyphenylene, diphenyl ether, phenanthrene, diaryl compound, triaryl compound, diaryl ether, triaryl ether, alkyl aryl compound, alkyl aryl compound, Diarylalkyl compounds or combinations thereof.

The first flowable heat transfer medium can have any suitable temperature. For example, the first flowable heat transfer medium can be from about 20 ° C to 400 ° C, or from about 50 ° C to 350 ° C, from 100 ° C to 300 ° C, from 100 ° C to 200 ° C, from 200 ° C to 250 ° C, or from about 250 ° C. Up to 300 ° C, or about 20 ° C or below, or about 30 ° C, 40 ° C, 50 ° C, 60 ° C, 70 ° C, 80 ° C, 90 ° C, 100 ° C, 110 ° C, 120 ° C, 130 ° C, 140 ° C , 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 ° C, 300 ° C, 310 °C, 320 ° C, 330 ° C, 340 ° C, 350 ° C, 360 ° C, 370 ° C, 380 ° C, 390 ° C or about 400 ° C or above. The first flowable heat transfer medium can have any suitable phase, such as a gas phase, a liquid phase, or any suitable combination thereof. For example, the first flowable heat transfer medium can be about 60% by weight or less, or about 70% by weight, 80% by weight, 85% by weight, 90% by weight, 95% by weight, 96% by weight, 97. A liquid phase of wt%, 98 wt% or about 99 wt% or more. The first flowable heat transfer medium can be a substantially liquid phase.

The heated first flowable heat transfer medium can have any suitable temperature. For example, the heated first flowable heat transfer medium can be from about 100 ° C to 500 ° C, from 100 ° C to 400 ° C, from 100 ° C to 300 ° C, from 100 ° C to 200 ° C, from 200 ° C to 250 ° C, from 250 ° C to 300 ° C, 300 ° C to 350 ° C, 350 ° C to 400 ° C, 400 ° C to 500 ° C, 280 ° C to 400 ° C, or 330 ° C to 350 ° C, or about 100 ° C or less, or about 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C 290 ° C, 300 ° C, 310 ° C, 320 ° C, 330 ° C, 340 ° C, 350 ° C, 360 ° C, 370 ° C, 380 ° C, 390 ° C or about 400 ° C or above. The heated first flowable heat transfer medium can have any suitable phase, such as a gas phase, a liquid phase, or any suitable combination thereof. For example, the heated first flowable heat transfer medium can be about 60% by weight or less, or about 70% by weight, 80% by weight, 85% by weight, 90% by weight, 95% by weight, 96% by weight. %, 97% by weight, 98% by weight or about 99% by weight or more of the liquid phase. The heated first flowable heat transfer medium can be a substantially liquid phase.

During heating of the first flowable heat transfer medium, the first flowable heat transfer medium can be substantially maintained as a liquid (eg, substantially no vaporization of the first flowable heat transfer medium occurs). The heat transferred to the first flowable heat transfer medium during heating of the first flowable heat transfer medium can include substantially all of the sensible heat. For example, during heating of the first flowable heat transfer medium, the heat transferred to the first flowable heat transfer medium can include any suitable percentage of sensible heat, such as about 60% or less, or about 70%, 80. %, 85%, 90%, 95%, 96%, 97%, 98% or about 99% or more of sensible heat, the remainder being latent heat (eg heat of vaporization).

The heated first flowable heat transfer medium can be substantially maintained as a liquid during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium. For example, the first flowable heat transfer medium does not freeze. The heated first flowable heat transfer medium does not substantially condense during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium. For example, if the heated first flowable heat transfer medium is substantially liquid phase, condensation does not occur, or only the less gas phase components of the heated first flowable heat transfer medium condense. The heat transferred by the heated first flowable heat transfer medium may include substantially all of the sensible heat during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium. For example, during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium, the heat transferred by the heated first flowable heat transfer medium The amount can include any suitable percentage of sensible heat, such as about 60% or less, or about 70%, 80%, 85%, 90%, 95%, 96%, 97%, 98%, or about 99% or 99. More than sensible heat, the rest is latent heat (such as heat of vaporization).

Both the first flowable heat transfer medium and the heated first flowable heat transfer medium can be disposed in the first heating circuit. The use of the heated first flowable heat transfer medium to transfer heat to the second flowable heat transfer medium provides a used first flowable heat transfer medium. The method can include recycling the first flowable heat transfer medium to a state in which the first flowable heat transfer medium is heated. The first heating circuit may be a primary circuit that circulates the first heat transfer material between a central heating position in the facility and one or more secondary circuits containing the second flowable heat transfer medium, or the first heating circuit may be A primary circuit for, for example, heating less than all of the secondary circuits containing the second flowable heat transfer medium.

The method can include controlling at least one of a pressure of the first flowable heat transfer medium and a temperature of the heated first flowable heat transfer medium. Controlling the pressure of the first flowable heat transfer medium and controlling the pressure of the heated first flowable heat transfer medium can include controlling the pressure in the first heating circuit. The pressure can be controlled to any suitable pressure, such as from about 50 KPa to 1,000,000 KPa, from 100 KPa to 500,000 KPa, or from 500 KPa to 250,000 KPa, or from about 50 KPa or below, or from about 100 KPa, 500 KPa, 1 MPa, 2 MPa, 3 MPa, 4 MPa, 5 MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, 12.5MPa, 15MPa, 17.5MPa, 20MPa, 25MPa, 30MPa, 35MPa, 40MPa, 45MPa, 50MPa, 60MPa, 70MPa, 80MPa, 90MPa, 100MPa, 125MPa, 150MPa, 175MPa, 200MPa or About 250 MPa or more. In some examples, the saturation temperature can be controlled to any suitable temperature, such as from about 100 ° C to 500 ° C, from 100 ° C to 400 ° C, from 100 ° C to 300 ° C, from 100 ° C to 200 ° C, from 200 ° C to 250 ° C, from 250 ° C to 300 ° C, 300 ° C to 350 ° C, 350 ° C to 400 ° C, 400 ° C to 500 ° C, 210 ° C to 350 ° C, or 260 ° C to 300 ° C, or about 100 ° C or less, or about 110 ° C, 120 ° C , 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170°C, 180°C, 190°C, 200°C, 210°C, 220°C, 230°C, 240°C, 250°C, 260°C, 270°C, 280°C, 290°C, 300°C, 310°C, 320°C, 330°C 340 ° C, 350 ° C, 360 ° C, 370 ° C, 380 ° C, 390 ° C or about 400 ° C or above. The maximum temperature of the heated first flowable heat transfer medium may differ from the saturation temperature of the heated first flowable heat transfer medium by any suitable range, such as from the saturation temperature of the heated first flowable heat transfer medium About 0 ° C to 100 ° C, 0 ° C to 60 ° C, about 0 ° C to 40 ° C, or about 0 ° C, 1 ° C, 2 ° C, 3 ° C, 4 ° C, 5 ° C, 10 ° C, 15 ° C, 20 ° C, 25 °C, 30°C, 35°C, 40°C, 50°C, 60°C, 70°C, 80°C, 90°C or within about 100°C. In various embodiments, the pressure of the first flowable heat transfer medium and the heated first flowable heat transfer medium can be similarly controlled to control the first flowable heat transfer in the example including vaporizing the first heat transfer medium. The saturation temperature of the medium. Controlling the temperature at which the first flowable heat transfer medium vaporizes and the temperature at which the heated first flowable heat transfer medium condenses (e.g., saturation temperature) controls the temperature of the heated second flowable heat transfer medium.

The first flowable heat transfer medium and the heated first flowable heat transfer medium can independently have any suitable vapor pressure, such as from about 50 KPa to 1,000,000 KPa, from 100 KPa to 500,000 KPa, or from 500 KPa to 250,000 KPa, or from about 50 KPa or 50 KPa. Hereinafter, or about 100KPa, 500KPa, 1MPa, 2MPa, 3MPa, 4MPa, 5MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, 12.5MPa, 15MPa, 17.5MPa, 20MPa, 25MPa, 30MPa, 35MPa, 40MPa, 45MPa, 50MPa, 60 MPa, 70 MPa, 80 MPa, 90 MPa, 100 MPa, 125 MPa, 150 MPa, 175 MPa, 200 MPa or about 250 MPa or more.

The first flowable heat transfer medium and the heated first flowable heat transfer medium can have any suitable heat capacity. For example, at about 100 ° C or below, or at about 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C , 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 ° C, 300 ° C, 310 ° C, 320 ° C, 330 ° C, 340 ° C, 350 ° C, The heat capacity of the first flowable heat transfer medium and the heated first flowable heat transfer medium may be from 0.2 KJ/Kg ° C to about 360 ° C, 370 ° C, 380 ° C, 390 ° C or above about 400 ° C or above. 8.5 KJ/Kg ° C, from about 1 KJ/Kg ° C to about 4 KJ/Kg ° C, about 0.2 KJ/Kg ° C or less than 0.2 KJ/Kg ° C, or about 0.5 KJ/Kg ° C, 1 KJ/Kg ° C, 1.1 KJ/Kg ° C 1.2KJ/Kg°C, 1.3KJ/Kg°C, 1.4KJ/Kg°C, 1.5KJ/Kg°C, 1.6KJ/Kg°C, 1.7KJ/Kg°C, 1.8KJ/Kg°C, 1.9KJ/Kg°C, 2KJ /Kg°C, 2.1KJ/Kg°C, 2.2KJ/Kg°C, 2.3KJ/Kg°C, 2.4KJ/Kg°C, 2.5KJ/Kg°C, 2.6KJ/Kg°C, 2.7KJ/Kg°C, 2.8KJ/Kg °C, 2.9KJ/Kg°C, 3KJ/Kg°C, 3.1KJ/Kg°C, 3.2KJ/Kg°C, 3.5KJ/Kg°C, 4KJ/Kg°C, 4.5KJ/Kg°C, 5KJ/Kg°C, 5.5KJ/ Kg ° C, 6 KJ / Kg ° C, 6.5 KJ / Kg ° C, 7 KJ / Kg ° C, 7.5 KJ / Kg ° C, 8 KJ / Kg ° C or about 8.5 KJ / Kg ° C or 8.5 KJ / Kg ° C or more.

The first flowable heat transfer medium can be cycled at any suitable rate, such as from about 1 L/min to about 1,000,000 L/min, or from about 10 L/min to about 100,000 L/min, or about 1 L/min or less, 10 L/ Min, 20L/min, 30L/min, 40L/min, 50L/min, 60L/min, 70L/min, 80L/min, 90L/min, 100L/min, 125L/min, 150L/min, 175L/min, 200L/min, 225L/min, 250L/min, 275L/min, 300L/min, 350L/min, 400L/min, 450L/min, 500L/min, 600L/min, 700L/min, 800L/min, 900L/ Min, 1,000 L/min, 2,500 L/min, 5,000 L/min, 10,000 L/min, 50,000 L/min, 100,000 L/min, 500,000 L/min or about 1,000,000 L/min or more than 1,000,000 L/min.

Second flowable heat transfer medium.

In the method, system or apparatus, the second flowable heat transfer medium can be any suitable flowable heat transfer medium. The second flowable heat transfer medium can include one or more organic compounds having characteristics that make the second flowable heat transfer medium suitable for use in the methods, systems, and devices described herein. The second heat transfer medium flow may be for example, water, polyethylene glycol, polypropylene glycol, mineral oil, polyethylene oxide silicone oil, diphenyl ether, biphenyl, terphenyl, THERMINOL ^® brand heat transfer fluid and DOWTHERM ^TM brand At least one of the hot fluids. The second heat transfer medium may flow may comprise e.g. DOWTHERM ^TM brand heat transfer fluid, such as at least one of: DOWTHERM ^TM A (e.g. diphenyl ether and biphenyl, for example a eutectic mixture of biphenyl and diphenyl ether, 26.5 wt e.g. % and 73.5 wt.% diphenyl ether), DOWTHERM ^TM G (e.g. diaryl compounds, triarylmethane compounds, diaryl and triaryl ether), DOWTHERM ^TM J (e.g. alkyl aryl compounds), DOWTHERM ^TM MX (e.g. alkyl aryl compounds), DOWTHERM ^TM Q (e.g. ethane, alkylaryl compound), DOWTHERM ^TM RP (e.g. diaryl alkyl compound) and DOWTHERM ^TM T (C _14-30 e.g. Alkylbenzene). The second flowable heat transfer medium may include, for example, trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _14-30 alkyl aryl compound, diethylbenzene, vinylated benzene, cyclohexyl Benzene, C _14-30 alkyl benzene, white petroleum mineral oil, ethyl diphenylethane, diphenylethane, diethyl diphenylethane, diphenyl ether, diphenyl oxide , ethyl benzene polymer, biphenyl, inorganic salt, diisopropyl biphenyl, triisopropyl biphenyl, methyl cyclohexane, bicyclohexane, terphenyl, hydrogenated terphenyl, partial hydrogenation couplet Tetrabenzene, partially hydrogenated high carbon polyphenylene, diphenyl ether, phenanthrene, diaryl compound, triaryl compound, diaryl ether, triaryl ether, alkyl aryl compound, alkyl aryl compound, Diarylalkyl compounds or combinations thereof.

The second flowable heat transfer medium can have any suitable temperature. For example, the second flowable heat transfer medium can be from about 20 ° C to 400 ° C, or from about 50 ° C to 350 ° C, from 100 ° C to 300 ° C, from 100 ° C to 200 ° C, from 200 ° C to 250 ° C, or from about 250 ° C. Up to 300 ° C, or about 20 ° C or below, or about 30 ° C, 40 ° C, 50 ° C, 60 ° C, 70 ° C, 80 ° C, 90 ° C, 100 ° C, 110 ° C, 120 ° C, 130 ° C, 140 ° C , 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 ° C, 300 ° C, 310 °C, 320 ° C, 330 ° C, 340 ° C, 350 ° C, 360 ° C, 370 ° C, 380 ° C, 390 ° C or about 400 ° C or above. The second flowable heat transfer medium can have any suitable phase, such as a gas phase, a liquid phase, or any What is suitable for combination. For example, the second flowable heat transfer medium can be about 60% by weight or less, or about 70% by weight, 80% by weight, 85% by weight, 90% by weight, 95% by weight, 96% by weight, 97. A gas phase of wt%, 98 wt% or about 99 wt% or more. The second flowable heat transfer medium can be substantially gas phase.

The heated second flowable heat transfer medium can have any suitable temperature. For example, the heated second flowable heat transfer medium can be from about 100 ° C to 500 ° C, from 100 ° C to 400 ° C, from 100 ° C to 300 ° C, from 100 ° C to 200 ° C, from 200 ° C to 250 ° C, from 250 ° C to 300 ° C, 300 ° C to 350 ° C, 350 ° C to 400 ° C, 400 ° C to 500 ° C, 210 ° C to 350 ° C, or 260 ° C to 300 ° C, or about 100 ° C or less, or about 110 ° C, 120 ° C , 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 °C, 300°C, 310°C, 320°C, 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C or about 400°C or above. The heated second flowable heat transfer medium can have any suitable phase, such as a gas phase, a liquid phase, or any suitable combination thereof. For example, the heated second flowable heat transfer medium can be about 60% by weight or less, or about 70% by weight, 80% by weight, 85% by weight, 90% by weight, 95% by weight, 96% by weight. %, 97% by weight, 98% by weight or about 99% by weight or more by weight of the gas phase. The heated second flowable heat transfer medium can be substantially gaseous.

The second flowable heat transfer medium may substantially become a gas during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium (eg, the second flowable heat transfer medium may be substantially all Vaporization). During transfer of heat from the heated first flowable heat transfer medium to the second flowable heat transfer medium, the heat transferred to the second flowable heat transfer medium may include substantially all latent heat (eg, heat of vaporization). For example, during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium, the heat transferred to the second flowable heat transfer medium can include any suitable percentage of latent heat, such as about 60 % to 100%, 70% to 100%, 80% to 100%, 90% to 100%, or about 60% or less, or about 65%, 70%, 75%, 80%, 85%, 90%, 95%, 96%, 97%, 98% or about 99% or more than 99% to latent heat (eg heat of vaporization), the balance being sensible heat.

The heated second flowable heat transfer medium can be substantially condensed into a liquid during heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system. For example, substantially all of the gas phase of the heated second flowable heat transfer medium can condense. During heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system, the heat transferred by the second flowable heat transfer medium can include substantially all latent heat (e.g., heat of vaporization). During heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system, the heat transferred by the second flowable heat transfer medium may comprise any suitable percentage of latent heat, such as about 60% Up to 100%, 70% to 100%, 80% to 100%, 90% to 100%, or about 60% or less, or about 65%, 70%, 75%, 80%, 85%, 90% , 95%, 96%, 97%, 98% or about 99% or more of latent heat (such as heat of vaporization), the rest being sensible heat.

The method can include controlling a pressure of the second flowable heat transfer medium and controlling a pressure of the heated second flowable heat transfer medium to control a temperature at which the second flowable heat transfer medium vaporizes and controlling the heated second flowable medium The temperature at which the heat medium condenses. The second heat transfer medium and the heated second heat transfer medium can be disposed in the second heating circuit. Heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system provides a used second flowable heat transfer medium. The method can include recycling the used second flowable heat transfer medium back to a state of heat transfer from the heated first flowable heat transfer medium.

Controlling the pressure of the second flowable heat transfer medium and controlling the pressure of the heated second flowable heat transfer medium can include controlling the pressure in the second heating circuit. The pressure can be controlled to any suitable pressure, such as from about 50 KPa to 1,000,000 KPa, from 100 KPa to 500,000 KPa, or from 500 KPa to 250,000 KPa, or from about 50 KPa or below, or from about 100 KPa, 500 KPa, 1 MPa, 2 MPa, 3 MPa, 4 MPa, 5 MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, 12.5MPa, 15MPa, 17.5MPa, 20 MPa, 25 MPa, 30 MPa, 35 MPa, 40 MPa, 45 MPa, 50 MPa, 60 MPa, 70 MPa, 80 MPa, 90 MPa, 100 MPa, 125 MPa, 150 MPa, 175 MPa, 200 MPa or about 250 MPa or 250 MPa or more. In some examples, the saturation temperature can be controlled to any suitable temperature, such as from about 100 ° C to 500 ° C, from 100 ° C to 400 ° C, from 100 ° C to 300 ° C, from 100 ° C to 200 ° C, from 200 ° C to 250 ° C, from 250 ° C to 300 ° C, 300 ° C to 350 ° C, 350 ° C to 400 ° C, 400 ° C to 500 ° C, 210 ° C to 350 ° C, or 260 ° C to 300 ° C, or about 100 ° C or less, or about 110 ° C, 120 ° C , 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 °C, 300°C, 310°C, 320°C, 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C or about 400°C or above. The maximum temperature of the heated second flowable heat transfer medium may differ from the saturation temperature of the heated second flowable heat transfer medium by any suitable range, such as the saturation temperature of the heated second flowable heat transfer medium About 0 ° C to 100 ° C, 0 ° C to 60 ° C, about 0 ° C to 40 ° C, or about 0 ° C, 1 ° C, 2 ° C, 3 ° C, 4 ° C, 5 ° C, 10 ° C, 15 ° C, 20 ° C, 25 °C, 30°C, 35°C, 40°C, 50°C, 60°C, 70°C, 80°C, 90°C or within about 100°C. In various embodiments, the pressure of the first flowable heat transfer medium and the heated first flowable heat transfer medium can be similarly controlled to control the first flowable heat transfer in the example including vaporizing the first heat transfer medium. The saturation temperature of the medium.

Controlling the temperature at which the second flowable heat transfer medium vaporizes and the temperature at which the heated second flowable heat transfer medium condenses (e.g., saturation temperature) controls the temperature of the tubular reactor of the polyamine synthesis system. The temperature of the tubular reactor of the polyamine synthesis system can be controlled to any suitable temperature, such as from about 100 ° C to 500 ° C, from 100 ° C to 400, by controlling the pressure and thereby controlling the saturation temperature of the second flowable heat transfer medium. °C, 100 ° C to 300 ° C, 100 ° C to 200 ° C, 200 ° C to 250 ° C, 250 ° C to 300 ° C, 300 ° C to 350 ° C, 350 ° C to 400 ° C, 400 ° C to 500 ° C, 210 ° C to 350 ° C, Or 260 ° C to 300 ° C, or about 100 ° C Or 100 ° C or less, or about 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 °C, 260°C, 270°C, 280°C, 290°C, 300°C, 310°C, 320°C, 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C or about 400°C or 400°C the above.

The second flowable heat transfer medium and the heated second flowable heat transfer medium can independently have any suitable vapor pressure, such as from about 50 KPa to 1,000,000 KPa, from 100 KPa to 500,000 KPa, or from 500 KPa to 250,000 KPa, or from about 50 KPa or 50 KPa. Hereinafter, or about 100KPa, 500KPa, 1MPa, 2MPa, 3MPa, 4MPa, 5MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, 12.5MPa, 15MPa, 17.5MPa, 20MPa, 25MPa, 30MPa, 35MPa, 40MPa, 45MPa, 50MPa, 60 MPa, 70 MPa, 80 MPa, 90 MPa, 100 MPa, 125 MPa, 150 MPa, 175 MPa, 200 MPa or about 250 MPa or more.

The second flowable heat transfer medium and the heated second flowable heat transfer medium can have any suitable heat capacity. For example, at about 100 ° C or below, or at about 110 ° C, 120 ° C, 130 ° C, 140 ° C, 150 ° C, 160 ° C, 170 ° C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 ° C, 300 ° C, 310 ° C, 320 ° C, 330 ° C, 340 ° C, 350 ° C, 360 ° C, 370 ° C, 380 ° C, 390 At or above about 400 ° C or above, the second flowable heat transfer medium and the heated second flowable heat transfer medium may have a heat capacity of from 0.2 KJ/Kg ° C to about 8.5 KJ/Kg ° C, about 1 KJ/Kg. °C to about 4KJ/Kg°C, about 0.2KJ/Kg°C or less than 0.2KJ/Kg°C, or about 0.5KJ/Kg°C, 1KJ/Kg°C, 1.1KJ/Kg°C, 1.2KJ/Kg°C, 1.3KJ/ Kg ° C, 1.4 KJ / Kg ° C, 1.5 KJ / Kg ° C, 1.6 KJ / Kg ° C, 1.7 KJ / Kg ° C, 1.8 KJ / Kg ° C, 1.9 KJ / Kg ° C, 2 KJ / Kg ° C, 2.1 KJ / Kg ° C, 2.2KJ/Kg°C, 2.3KJ/Kg°C, 2.4KJ/Kg°C, 2.5KJ/Kg°C, 2.6KJ/Kg°C, 2.7KJ/Kg°C, 2.8KJ/Kg°C, 2.9KJ/Kg°C, 3KJ/ Kg°C, 3.1 KJ/Kg°C, 3.2KJ/Kg°C, 3.5KJ/Kg°C, 4KJ/Kg°C, 4.5KJ/Kg°C, 5KJ/Kg°C, 5.5KJ/Kg°C, 6KJ/Kg°C, 6.5KJ/Kg°C, 7KJ/Kg ° C, 7.5 KJ/Kg ° C, 8 KJ/Kg ° C or about 8.5 KJ/Kg ° C or 8.5 KJ/Kg ° C or more.

The temperature difference between the heated first flowable heat transfer medium and the heated second flowable heat transfer medium can be any suitable difference; for example, the difference can be from about 0 ° C to 300 ° C, from 0 ° C to 200 ° C. , 0 ° C to 100 ° C, 0 ° C to 60 ° C, about 0 ° C to 40 ° C, or about 0 ° C, 1 ° C, 2 ° C, 3 ° C, 4 ° C, 5 ° C, 10 ° C, 15 ° C, 20 ° C, 25 °C, 30°C, 35°C, 40°C, 50°C, 60°C, 70°C, 80°C, 90°C, 100°C, 110°C, 120°C, 130°C, 140°C, 150°C, 160°C, 170°C, 180 ° C, 190 ° C, 200 ° C, 210 ° C, 220 ° C, 230 ° C, 240 ° C, 250 ° C, 260 ° C, 270 ° C, 280 ° C, 290 ° C or about 300 ° C or more. The temperature difference between the first flowable heat transfer medium and the heated first flowable heat transfer medium and the temperature difference between the second flowable heat transfer medium and the heated second flowable heat transfer medium may be any suitable Difference; for example, the difference may independently be about 0 ° C to 300 ° C, 0 ° C to 200 ° C, 0 ° C to 100 ° C, 0 ° C to 60 ° C, about 0 ° C to 40 ° C, or about 0 ° C, 1 ° C, 2 °C, 3°C, 4°C, 5°C, 10°C, 15°C, 20°C, 25°C, 30°C, 35°C, 40°C, 50°C, 60°C, 70°C, 80°C, 90°C, 100°C, 110°C, 120°C, 130°C, 140°C, 150°C, 160°C, 170°C, 180°C, 190°C, 200°C, 210°C, 220°C, 230°C, 240°C, 250°C, 260°C, 270°C , 280 ° C, 290 ° C or about 300 ° C or more.

The second flowable heat transfer medium can be cycled at any suitable rate, such as from about 1 L/min to about 1,000,000 L/min, or from about 10 L/min to about 100,000 L/min, or about 1 L/min or less, 10 L/ Min, 20L/min, 30L/min, 40L/min, 50L/min, 60L/min, 70L/min, 80L/min, 90L/min, 100L/min, 125L/min, 150L/min, 175L/min, 200L/min, 225L/min, 250L/min, 275L/min, 300L/min, 350L/min, 400L/min, 450L/min, 500L/min, 600L/min, 700L/min, 800L/min, 900L/ Min, 1,000L/min, 2,500 L/min, 5,000 L/min, 10,000 L/min, 50,000 L/min, 100,000 L/min, 500,000 L/min or about 1,000,000 L/min or more than 1,000,000 L/min.

Other flowable heat transfer media.

In the method, system or apparatus, heat from the heated first flowable heat transfer medium can be transferred to one or more second flowable heat transfer media. For example, a first heating circuit containing a first flowable heat transfer medium can be used to heat a plurality of other heating circuits each containing a second flowable heat transfer medium. In another example, a first heating circuit comprising a first flowable heat transfer medium can be used to heat one or more second heating circuits each containing a second flowable heat transfer medium and each containing a third flowable heat transfer medium One or more third heating circuits.

The use of the heated first flowable heat transfer medium to transfer heat to the second flowable heat transfer medium provides a used first flowable heat transfer medium. The method can include transferring heat from the used first flowable heat transfer medium (eg, in series configuration) or from the heated first flowable heat transfer medium (eg, in a parallel configuration) to the third flowable heat transfer medium to provide A third flowable heat transfer medium that is heated. The method can include transferring heat from the third flowable heat transfer medium to at least one polyamine-containing component of the polyamine synthesis system. The third flowable heat transfer medium can be any suitable heat transfer medium described herein. The third flowable heat transfer medium can be the same or different than the second heat transfer medium. At least one component of the polyamine synthesis system that is heat transferred by the heated third flowable heat transfer medium and at least one component of the polyamine synthesis system that is heat transferred by the heated second flowable heat transfer medium Same or different.

Polyamine

The polyamine produced by the method, system or device can be any suitable polyamine. The polyamine can be synthesized from a linear dicarboxylic acid and a linear diamine or an oligomer formed from a linear dicarboxylic acid and a linear diamine. The polyamine can be nylon-6,6.

The dicarboxylic acid can be any suitable dicarboxylic acid. The dicarboxylic acid may have the structure HOC(O)-R ¹ -C(O)OH, wherein R ¹ is a C ₁ -C ₁₅ alkylene group such as methylene, ethyl, propyl, butyl, Stretching pentyl, stretching hexyl, stretching heptyl, stretching octyl, stretching sputum or stretching sputum. The dicarboxylic acid can be adipic acid (e.g., R ¹ = butyl).

The diamine can be any suitable diamine. The diamine may have the structure H ₂ NR ² —NH ₂ , wherein R ² is a C ₁ -C ₁₅ alkylene group, such as methylene, ethyl, propyl, butyl, pentyl, hexyl, Stretching the base, stretching the octyl group, stretching the base or stretching the base. The diamine can be adipic acid (e.g., R ² = butyl).

Instance

This creation can be more fully understood by reference to the examples provided below by way of illustration. This creation is not limited to the examples given herein.

A general method for determining the gelation rate. The gelation rates described in the examples were determined by taking the average of the gelation rates as determined by the two methods. In the first method, when the reaction mixture is still hot, the system is allowed to drain the liquid reaction mixture, the system is cooled, disassembled, and visually inspected to estimate the volume of the gel therein. In the second method, when the reaction mixture is still hot, the system is allowed to drain the liquid reaction mixture, cooled, filled with water and drained. The volume of gel in the system is determined by subtracting the volume of water discharged from the system from the gel-free volume of the system. To determine the rate of gelation downstream of one or more specific parts or specific locations of the equipment, only the specific parts of the equipment or downstream of the specific location of the system are filled with water. In both methods, the density of the gel was estimated to be 0.9 g/cm ³ .

Example 1a. Comparative example. Liquid phase heat transfer medium in the primary heating circuit.

Was heated in the apparatus for producing nylon-6,6 THERMINOL ^® 66 to about 340 ℃ and circulated through a heating loop. A heating loop so THERMINOL ^® 66 to fit between the heat exchanger on the circulating flow rate of the engine room and the evaporator, and the finisher reactor, after which the power THERMINOL ^® 66 is passed back to the heating chamber again. Use approximately 10,000,000 L of THERMINOL ^® 66 in the primary heating circuit. THERMINOL ^® 66 remains liquid throughout the process.

In a continuous nylon-6,6 manufacturing process, adipic acid and hexamethylenediamine are combined in water at about the same molar ratio to form an aqueous mixture containing nylon-6,6 salt and having about 50% by weight water. The brine solution was passed to the evaporator at about 105 L/min. The heat transfer from the THERMINOL ^® 66 in the primary heating circuit to the evaporator causes the evaporator to heat the brine solution to a temperature of about 125 ° C to 135 ° C (130 ° C) and remove the water from the heated brine solution to a water concentration of about 30 weight. %. The evaporated salt mixture was passed to the tubular reactor at about 75 L/min. The tubular reactor has a length of about 40 m, an average inner diameter of about 89 cm, an inner diameter expansion ratio from the entry end to the exit end of about 2.5 cm every 5 m length, an L/D ratio of about 45, and a distribution along the length. Discharge. Heat transfer from the reactor to THERMINOL ^® 66 in the primary heating circuit to bring the temperature of the evaporated salt mixture to between about 218 ° C and 250 ° C (235 ° C) to further remove water from the heated salt mixture of the reactor. Thereby the water concentration is brought to about 10% by weight and the salt is further polymerized. The reaction mixture was passed to the flasher at about 60 L/min. Heat transfer from THERMINOL ^® 66 in the primary heating circuit to the flasher, heating the reaction mixture to a temperature of about 270 ° C to 290 ° C (280 ° C), allowing the flasher to further remove water from the reaction mixture, thereby achieving a water concentration About 0.5% by weight, and the reaction mixture was further polymerized. The flashed mixture was passed to the finishing machine at about 54 L/min, and the polymerization mixture was subjected to a vacuum to further remove water so that the water concentration reached about 0.1% by weight, so that the polyamidamine reached a suitable final degree of polymerization range, after which The refined polymerization mixture is passed to an extruder and a granulator.

The liquid THERMINOL ^® 66 requires a large pump to circulate the material throughout the primary heating circuit to all unit operations and back to the power chamber for reheating. The total temperature of THERMINOL ^® 66 varies per kilogram of heat transferred by THERMINOL ^® 66 compared to other methods of heat transfer materials that undergo phase change during heat transfer; higher cycle rates and higher heat are used The exchanger heats the surface area to achieve the desired amount of heat transfer. In addition, it is difficult to maintain the precise temperature of each unit operation because the temperature of the heat transfer medium can only be adjusted overall and cannot be adjusted for individual units.

The three discharge ports distributed along the 40m reactor will generate a high pressure steam pool and make the liquid bureau Flashing, creating a plug flow regime, reducing the proportion of the annular flow and making it difficult to control the pressure. The plug flow and flashing cause the flow rate of the reaction mixture through the reactor to be non-uniform. The rapid expansion of the diameter causes the gel in the tubular reactor to solidify (e.g., freeze) the reaction mixture and cause excess water to be removed, thereby causing the flasher to undergo gas flow instability, freezing and vibration of the reaction mixture.

Example 1b. Comparative example. Gas phase heat transfer medium in the primary heating circuit.

In the apparatus for producing nylon-6,6, and at about 340 ℃ pressure of about 400KPa DOWTHERM ^TM A and heated to a vapor via a heated circulation circuit between the power chamber and the operation of various units, wherein the various unit operations which transfer Then, it is transferred back to the power chamber for heating. Using about 10,000,000L DOWTHERM ^TM A. In a heating loop Throughout the manufacturing process remains in DOWTHERM ^TM A vapor, and the material is sufficient to cause the circulation rate does not fall below the saturation temperature of the cycle.

As described in Example 1a nylon-6,6 in the continuous manufacturing processes, but using vaporization DOWTHERM ^TM A. throughout the manufacturing process Compared with other methods of heat transfer material undergoes a phase change heat transfer during use, the overall temperature of the DOWTHERM ^TM A A heat transfer per kJ per kg of DOWTHERM ^TM cause larger changes of; use a higher circulation rate and a large heat The exchanger heats the surface area to achieve the desired amount of heat transfer. In addition, it is difficult to maintain a precise temperature for each unit operation, such as a tubular reactor, since the temperature of the heat transfer medium can only be adjusted overall and cannot be adjusted for individual units.

Example 1c. Comparative example. Volatile heat transfer medium in a one-stage heating loop where condensation occurs.

According to Example 1b, but that to absorb enough heat from the heat during the operation of various units in DOWTHERM ^TM A circulating a heating rate A partial condensation of the circuit used DOWTHERM ^TM DOWTHERM ^TM A. In order to circulate the resulting liquid to the remaining unit operations and to recycle back to the power chamber, additional equipment, including liquid separation drums, other piping and pumps, is required to return the condensate to the power chamber for reheating and revaporization. It is difficult to maintain a precise temperature for each unit operation, such as a tubular reactor, since the temperature of the heat transfer medium can only be adjusted overall and cannot be adjusted for individual units.

Example 1d. Comparative example. Volatile heat transfer medium in a one-stage heating circuit with a leak point.

Follow example 1b. A leak occurs in the primary heating circuit. Since a high-pressure steam heating loop, so DOWTHERM ^TM A vapor leakage through the leak, so that the entire heating circuit of a reduced pressure. Due to the size of the primary heating circuit, a large amount of vapor leaks through the leak point, after which the pressure in the system drops to a level that slows the leak rate. At and around the leak (including an area near the connection of the fluid leak gap and the air gap), the leakage of the vapor present DOWTHERM ^TM A fire or explosion risk. In order for the leak to stop or extinguish the fire caused by the leak, the entire primary heating circuit in the equipment must be shut down.

Example 1e. Comparative example. Volatile heat transfer medium in a one-stage heating circuit with a leak.

Follow example 1c. A leak occurs in the primary heating circuit. Since a high-pressure steam heating loop, so DOWTHERM ^TM A vapor leakage through the leak, so that the entire heating circuit of a reduced pressure. Due to the size of the primary heating circuit, a large amount of vapor leaks through the leak point, after which the pressure in the system drops to a level that slows the leak rate. At and around the leak (including an area near the connection of the fluid leak gap and the air gap), the leakage of the vapor present DOWTHERM ^TM A fire or explosion risk. In order for the leak to stop or extinguish the fire caused by the leak, the entire primary heating circuit in the equipment must be shut down.

Example 2a. THERMINOL® 66 in an evaporator, tubular reactor, and flasher primary heating loop heated via a secondary heating loop.

In the manufacturing apparatus nylon-6,6 THERMINOL ^® 66 is heated to about 340 ℃ and circulated through a heating loop. The primary heating circuit circulates THERMINOL ^® 66 between the power chamber and the heat exchanger on the secondary heating circuit and some individual unit operated heat exchangers. Secondary heating loop containing DOWTHERM ^TM A, and used to heat the evaporator, reactor and flasher. Independently adjusting the pressure of the secondary heating circuit to change the temperature of vaporization and condensation DOWTHERM ^TM A precise control of each specific operating cell temperature of the heating. The primary heating loop contains approximately 10,000,000 L of THERMINOL ^® 66 and each secondary heating loop contains approximately 50,000 L of DOWTHERM ^TM A.

In a continuous nylon-6,6 manufacturing process, adipic acid and hexamethylenediamine are combined in water at about the same molar ratio to form an aqueous mixture containing nylon-6,6 salt having about 50% by weight water. The brine solution was passed to the evaporator at about 105 L/min. A secondary heating circuit is used as the evaporator in the DOWTHERM ^TM A heat transfer to the evaporator, the evaporator the aqueous salt solution is heated to about 125 ℃ to 135 ℃ (130 ℃) and heating the aqueous solution of the salt is removed from the water, so that The water concentration reached about 30% by weight. The pressure of the secondary heating loop on the evaporator was adjusted to between about 1 KPa and about 3 KPa (2 KPa ^{) to} maintain the saturation temperature of DOWTHERMTM A at about 130 °C. The evaporated salt mixture was passed to the tubular reactor at about 75 L/min. The tubular reactor has a length of about 40 m, an average inner diameter of about 89 cm, an inner diameter expansion ratio from the inlet end to the exit end of about 2.5 cm, a L/D ratio of about 45, and a distribution along the length of about 2.5 cm every 5 m. Discharge. Heating the salt mixture composed of a secondary circuit of a reactor in the DOWTHERM ^TM A heat transfer to the reactor, the temperature of the salt mixture is evaporated to approximately 218 deg.] C to 250 ℃ (235 ℃), the reactor was heated from the evaporated The water is further removed so that the water concentration reaches about 10% by weight and the salt is further polymerized. The two heating circuit on the reactor pressure was adjusted to about 28KPa to about 97KPa (80KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 235 ℃. The reaction mixture was passed to the flasher at about 60 L/min. Of a secondary heating circuit flasher's in the DOWTHERM ^TM A heat transfer to the flasher, the reaction mixture of is heated to about 270 deg.] C to 290 ℃ (280 ℃), that the flasher further remove water from the reaction mixture of the Thereby, the water concentration is brought to about 0.5% by weight, and the reaction mixture is further polymerized. The pressure on the secondary heating circuit is adjusted to about flasher about 150KPa to 200KPa (180KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 280 ℃. The flashed mixture was passed to the finisher at about 54 L/min and the polymerization mixture was subjected to a vacuum to further remove water so that the water concentration reached about 0.1% by weight, allowing the polyamide to reach a suitable final degree of polymerization, after which The processed polymerization mixture is passed to an extruder and a granulator.

The three discharge ports distributed along the 40 m reactor produce a high pressure steam pool and partially flash the liquid, creating a plug flow regime, reducing the proportion of the annular flow and making it difficult to control the pressure. The plug flow and flashing cause the flow rate of the reaction mixture through the reactor to be non-uniform. The rapid expansion of the diameter causes the gel in the tubular reactor to solidify (e.g., freeze) the reaction mixture and cause excess water to be removed, thereby causing the flasher to undergo gas flow instability, freezing and vibration of the reaction mixture.

Example 2b. THERMINOL in a primary heating loop with an evaporator heated by a secondary heating loop, a tubular reactor, and a flasher ^® 66.

In the manufacturing apparatus nylon-6,6 THERMINOL ^® 66 is heated to about 340 ℃ and circulated through a heating loop. The primary heating circuit circulates THERMINOL ^® 66 between the power chamber and the heat exchanger on the secondary heating circuit and some individual unit operated heat exchangers. Secondary heating loop containing DOWTHERM ^TM A, and used to heat the evaporator, reactor and flasher. Independently adjusting the pressure of the secondary heating circuit to change the temperature of vaporization and condensation DOWTHERM ^TM A precise control of each specific operating cell temperature of the heating. The primary heating loop contains approximately 10,000,000 L of THERMINOL ^® 66 and each secondary heating loop contains approximately 50,000 L of DOWTHERM ^TM A.

In a continuous nylon-6,6 manufacturing process, adipic acid and hexamethylenediamine are combined in water at about the same molar ratio to form an aqueous mixture containing a nylon-6,6 salt and having a water concentration of about 50% by weight. The brine solution was passed to the evaporator at about 105 L/min. A secondary heating circuit is used as the evaporator in the DOWTHERM ^TM A heat transfer to the evaporator, the evaporator the aqueous salt solution is heated to about 125 ℃ to 135 ℃ (130 ℃) and heating the aqueous solution of the salt is removed from the water, so that The water concentration reached about 30% by weight. The pressure of the secondary heating loop on the evaporator was adjusted to between about 1 KPa and about 3 KPa (2 KPa ^{) to} maintain the saturation temperature of DOWTHERMTM A at about 130 °C. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, and the secondary heating circuit for the evaporator is compared with the saturation temperature of about 130 ° C. the temperature variation of DOWTHERM ^TM A is not higher or lower than about 15 ℃. The evaporated salt mixture was passed to the tubular reactor at about 75 L/min. The tubular reactor has a length of about 40 m, an average inner diameter of about 89 cm, an inner diameter expansion ratio from the inlet end to the exit end of about 2.5 cm, a L/D ratio of about 45, and a distribution along the length of about 2.5 cm every 5 m. Discharge. Heating the salt mixture composed of a secondary circuit of a reactor in the DOWTHERM ^TM A heat transfer to the reactor, the temperature of the salt mixture is evaporated to approximately 218 deg.] C to 250 ℃ (235 ℃), the reactor was heated from the evaporated The water is further removed so that the water concentration reaches about 10% by weight and the salt is further polymerized. The two heating circuit on the reactor pressure was adjusted to about 28KPa to about 97KPa (80KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 235 ℃. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, wherein the secondary heating for the evaporator is compared with the saturation temperature of about 235 ° C. temperature change circuit of DOWTHERM ^TM A sum is higher or lower is not more than about 15 ℃. The reaction mixture was passed to the flasher at about 60 L/min. Of a secondary heating circuit flasher's in the DOWTHERM ^TM A heat transfer to the flasher, the reaction mixture of is heated to about 270 deg.] C to 290 ℃ (280 ℃), that the flasher further remove water from the reaction mixture of the Thereby, the water concentration is brought to about 0.5% by weight, and the reaction mixture is further polymerized. The pressure on the secondary heating circuit is adjusted to about flasher about 150KPa to 200KPa (180KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 280 ℃. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, wherein the secondary heating for the evaporator is compared with a saturation temperature of about 280 °C. temperature change of the circuit of DOWTHERM ^TM A is higher or lower is not more than about 15 ℃. The flashed mixture was passed to the finisher at about 54 L/min and the polymerization mixture was subjected to a vacuum to further remove water so that the water concentration reached about 0.1% by weight, allowing the polyamide to reach a suitable final degree of polymerization, after which The processed polymerization mixture is passed to an extruder and a granulator.

The three discharge ports distributed along the 40 m reactor produce a high pressure steam pool and partially flash the liquid, creating a plug flow regime, reducing the proportion of the annular flow and making it difficult to control the pressure. The plug flow and flashing cause the flow rate of the reaction mixture through the reactor to be non-uniform. The rapid expansion of the diameter causes the gel in the tubular reactor to solidify (e.g., freeze) the reaction mixture and cause excess water to be removed, thereby causing the flasher to undergo gas flow instability, freezing and vibration of the reaction mixture.

Example 2c. THERMINOL in a one-stage heating circuit with an evaporator heated by a secondary heating loop, a tubular reactor, and a flasher ^® 66 and water used in the secondary circuit of the evaporator.

In the manufacturing apparatus nylon-6,6 THERMINOL ^® 66 is heated to about 340 ℃ and circulated through a heating loop. The primary heating circuit circulates THERMINOL ^® 66 between the power chamber and the heat exchanger on the secondary heating circuit and some individual unit operated heat exchangers. A secondary heating loop reactor and the flasher comprises DOWTHERM ^TM A. The secondary heating circuit for the evaporator contains water. Independently adjusting the pressure of the secondary heating circuit to change DOWTHERM ^TM A water vaporization or condensation temperature and to precisely control the operation of each specific cell temperature of heating. The primary heating loop contains approximately 10,000,000 L of THERMINOL ^® 66 and each secondary heating loop contains approximately 50,000 L of DOWTHERM ^TM A or water.

In a continuous nylon-6,6 manufacturing process, adipic acid and hexamethylenediamine are combined in water at about the same molar ratio to form an aqueous mixture containing a nylon-6,6 salt and having a water concentration of about 50% by weight. The brine solution was passed to the evaporator at about 105 L/min. A secondary heating circuit is used as the evaporator in the DOWTHERM ^TM A heat transfer to the evaporator, the evaporator the aqueous salt solution is heated to about 125 ℃ to 135 ℃ (130 ℃) and heating the aqueous solution of the salt is removed from the water, so that The water concentration reached about 30% by weight. The pressure of the secondary heating circuit on the evaporator was adjusted to about 270 KPa to maintain the water saturation temperature at about 130 °C. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, and the secondary heating circuit for the evaporator is compared with the saturation temperature of about 130 ° C. The temperature change of the water in the water becomes higher or lower and does not exceed about 15 °C. The evaporated salt mixture was passed to the tubular reactor at about 75 L/min. The tubular reactor has a length of about 40 m, an average inner diameter of about 89 cm, an inner diameter expansion ratio from the inlet end to the exit end of about 2.5 cm, a L/D ratio of about 45, and a distribution along the length of about 2.5 cm every 5 m. Discharge. Heating the salt mixture composed of a secondary circuit of a reactor in the DOWTHERM ^TM A heat transfer to the reactor, the temperature of the salt mixture is evaporated to approximately 218 deg.] C to 250 ℃ (235 ℃), the reactor was heated from the evaporated The water is further removed so that the water concentration reaches about 10% by weight and the salt is further polymerized. The two heating circuit on the reactor pressure was adjusted to about 28KPa to about 97KPa (80KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 235 ℃. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, wherein the secondary heating for the evaporator is compared with the saturation temperature of about 235 ° C. temperature change circuit of DOWTHERM ^TM A sum is higher or lower is not more than about 15 ℃. The reaction mixture was passed to the flasher at about 60 L/min. Of a secondary heating circuit flasher's in the DOWTHERM ^TM A heat transfer to the flasher, the reaction mixture of is heated to about 270 deg.] C to 290 ℃ (280 ℃), that the flasher further remove water from the reaction mixture of the Thereby, the water concentration is brought to about 0.5% by weight, and the reaction mixture is further polymerized. The pressure on the secondary heating circuit is adjusted to about flasher about 150KPa to 200KPa (180KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 280 ℃. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, wherein the secondary heating for the evaporator is compared with a saturation temperature of about 280 °C. temperature change of the circuit of DOWTHERM ^TM A is higher or lower is not more than about 15 ℃. The flashed mixture was passed to the finisher at about 54 L/min and the polymerization mixture was subjected to a vacuum to further remove water so that the water concentration reached about 0.1% by weight, allowing the polyamide to reach a suitable final degree of polymerization, after which The processed polymerization mixture is passed to an extruder and a granulator.

The three discharge ports distributed along the 40 m reactor produce a high pressure steam pool and partially flash the liquid, creating a plug flow regime, reducing the proportion of the annular flow and making it difficult to control the pressure. embolism The flow and flashing caused the flow rate of the reaction mixture through the reactor to be non-uniform. The rapid expansion of the diameter causes the gel in the tubular reactor to solidify (e.g., freeze) the reaction mixture and cause excess water to be removed, thereby causing the flasher to undergo gas flow instability, freezing and vibration of the reaction mixture.

Example 3. THERMINOL® 66 in a one-stage heating circuit with a reactor heated by a secondary heating loop and an evaporator heated by a primary heating loop and a flasher.

The nylon-6,6 manufacturing equipment heats THERMINOL® 66 to about 340 ° C and circulates through a primary heating loop. The primary heating circuit circulates THERMINOL® 66 between the power chamber and the heat exchanger on the secondary heating circuit and some individual unit operated heat exchangers. Secondary heating loop containing DOWTHERM ^TM A and used to heat the reactor. Independently adjusting the pressure of the secondary heating circuit to change the temperature of vaporization and condensation DOWTHERM ^TM A precise control of the temperature of the reactor. A heating loop contains about 10,000,000L THERMINOL® 66, and secondary heating loop contains about 50,000L DOWTHERM ^TM A.

In a continuous nylon-6,6 manufacturing process, adipic acid and hexamethylenediamine are combined in water at about the same molar ratio to form an aqueous mixture containing nylon-6,6 salt having about 50% by weight water. The brine solution was passed to the evaporator at about 105 L/min. The heat is transferred from the THERMINOL® 66 in the primary heating circuit to the evaporator, so that the evaporator heats the brine solution to about 125 ° C to 135 ° C (130 ° C) and removes the water from the heated brine solution to a water concentration of about 30 weight. %. The evaporated salt mixture was passed to the tubular reactor at about 75 L/min. The tubular reactor has a length of about 40 m, an average inner diameter of about 89 cm, an inner diameter expansion ratio from the inlet end to the exit end of about 2.5 cm, a L/D ratio of about 45, and a distribution along the length of about 2.5 cm every 5 m. Discharge. Heating the salt mixture composed of a secondary circuit of a reactor in the DOWTHERM ^TM A heat transfer to the reactor, the temperature of the salt mixture is evaporated to approximately 218 deg.] C to 250 ℃ (235 ℃), the reactor was heated from the evaporated The water is further removed so that the water concentration reaches about 10% by weight and the salt is further polymerized. The two heating circuit on the reactor pressure was adjusted to about 28KPa to about 97KPa (80KPa), so that the saturation temperature of the DOWTHERM ^TM A maintained at about 235 ℃. The heat transfer between the primary heating circuit and the secondary heating circuit and the heat transfer between the secondary heating circuit and the evaporator are mainly sensible heat, wherein the secondary heating for the evaporator is compared with the saturation temperature of about 235 ° C. temperature change circuit of DOWTHERM ^TM A sum is higher or lower is not more than about 15 ℃. The reaction mixture was passed to the flasher at about 60 L/min. Heat transfer from THERMINOL ^® 66 in the primary heating circuit to the flasher, heating the reaction mixture to a temperature of about 270 ° C to 290 ° C (280 ° C), allowing the flasher to further remove water from the reaction mixture, thereby achieving a water concentration About 0.5% by weight, and the reaction mixture was further polymerized. The flashed mixture was passed to the finisher at about 54 L/min and the polymerization mixture was subjected to a vacuum to further remove water so that the water concentration reached about 0.1% by weight, allowing the polyamide to reach a suitable final degree of polymerization, after which The processed polymerization mixture is passed to an extruder and a granulator.

Example 4. Tubular reactor with longer length and finer diameter.

According to Example 2a, an inner diameter expansion ratio from the inlet end to the exit end, an L/D ratio of about 246, and a length distribution were used with an inner diameter of about 100 m and an inner diameter of about 0.41 m, a length of about 2.54 cm every 5 m. Tubular reactor with 8 outlets.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time.

Example 5a. Tubular reactor with longer length and finer diameter.

According to Example 2a, an inner diameter expansion ratio from the inlet end to the exit end, an L/D ratio of about 246, and a length distribution of 8 with an inner diameter of about 100 m and an inner diameter of about 41 cm and a length of about 2.5 cm every 550 m were used. a tubular reactor with a discharge port.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby Less improper by-products are formed in the steam released by the reactor and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time.

Example 5b. Tubular reactor with longer length and finer diameter.

According to Example 2a, an inner diameter expansion ratio from the entry end to the exit end, an L/D ratio of about 246, and a length distribution were used with an average inner diameter of about 100 m and an average inner diameter of about 41 cm, a length of about 2.5 cm every 110 m. Tubular reactor with 8 outlets.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time. This increase in diameter reduces the generation and accumulation of gels and other impurities in the reactor, helping to maintain a larger proportion of the annular flow throughout the reactor. This rate of increase in diameter provides a pressure drop between the inlet and outlet of the reactor which results in more efficient and efficient removal of water from the reactor, thereby reducing or preventing solidification of the polymer mixture in the reactor.

Example 5c. Tubular reactor with longer length and finer diameter.

According to Example 2a, an inner diameter expansion ratio from the entry end to the exit end, an L/D ratio of about 246, and a length distribution were used with an average inner diameter of about 100 m and an average inner diameter of about 41 cm, a length of about 2.5 cm every 110 m. Tubular reactor with 8 outlets.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time. This increase in diameter reduces the generation and accumulation of gels and other impurities in the reactor, helping to maintain a larger proportion of the annular flow throughout the reactor. Straight The increase in diameter provides a pressure drop between the inlet and outlet of the reactor which allows for more efficient and efficient removal of water from the reactor, thereby reducing or preventing solidification of the polymer mixture in the reactor.

Example 5d. Tubular reactor with longer length and finer diameter.

According to Example 2a, an inner diameter expansion ratio from the entry end to the exit end, an L/D ratio of about 246, and a length distribution of 8 with an inner diameter of about 100 m and an inner diameter of about 41 cm and a length of about 2.5 cm every 1000 m were used. a tubular reactor with a discharge port.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time.

This increase in diameter compared to Examples 5b and 5c made the removal of water in the reactor less effective, requiring a greater amount of energy to remove the same amount of water.

Example 6a. Tubular reactor with an increased number of discharges.

According to Example 2a, tubular reactors having the same size but having 7 discharge ports distributed along the length were used.

In contrast to the examples 1a-e and 2a-2b, the tubular reactor with an increased number of discharge ports has a smaller amount of steam traveling through the reaction tubes at each of the predetermined positions, and the steam in the tubes moves at a lower speed. The reduction in vapor volume and velocity allows less polymer mixture to travel into the discharge line, thereby allowing the discharge line to operate smoothly between cleaning times for a longer period of time. An increased number of discharge ports with distributed spacing also helps prevent partial flashing of the liquid and embolic flow, thereby providing a more stable flow rate and a greater proportion of the annular flow.

Example 6b. A tubular reactor with an increased number of discharge ports and a small separation between some discharge ports.

According to Example 2a, a tubular reactor having the same size but having 7 discharge ports was used, in which 5 discharge ports were evenly distributed, and the remaining 2 discharge ports were separated by about 1 m in reaction. Near the middle of the device.

In contrast to the examples 1a-e and 2a-2b, the tubular reactor with an increased number of discharge ports has a smaller amount of steam traveling through the reaction tubes at each of the predetermined positions, and the steam in the tubes moves at a lower speed. The reduction in vapor volume and velocity allows less polymer mixture to travel into the discharge line, thereby allowing the discharge line to operate smoothly between cleaning times for a longer period of time. An increase in the number of discharge ports also helps prevent partial flashing of the liquid and embolic flow, thereby providing a more stable flow rate and a greater proportion of the annular flow. However, the small spacing between the discharge ports clustered in the middle of the reactor destroys the annular flow in the region of the reactor; instead, the flow of the liquid is similar to the semi-cylinder located in the lower half of the tube, the remainder of the horizontal tube It is gas and steam. The reduced ratio of the annular flow results in a lower efficiency of heat transfer to the reaction mixture in the tube.

Example 6c. Excessive tubular reactor for discharge.

According to Example 2a, a tubular reactor of the same size but having 40 discharge ports distributed along its length was used.

In contrast to the examples 1a-e and 2a-2b, the tubular reactor with an increased number of discharge ports has a smaller amount of steam traveling through the reaction tubes at each of the predetermined positions, and the steam in the tubes moves at a lower speed. The reduction in vapor volume and velocity allows less polymer mixture to travel into the discharge line, thereby allowing the discharge line to operate smoothly between cleaning times for a longer period of time.

However, the small spacing between the discharge ports destroys the annular flow over the entire length of the reactor; instead, the flow of liquid is similar to the semi-cylindrical portion located in the lower half of the tube, with the remainder of the horizontal tube being gas and steam. The reduced ratio of the annular flow results in a lower efficiency of heat transfer to the reaction mixture in the tube.

Example 7. Tubular reactor using a water injection cleaning method.

According to Example 2a, a drain cleaning method was used in which water was injected into the discharge line to help prevent gel accumulation in the discharge line.

Compared to Examples 1a-e and 2a-2b, the tubular reactor operates for a longer period of time between the necessary cleaning and the unobstructed discharge.

Example 8a. Tubular reactor with longer length and finer diameter and increased number of discharge ports, using a water injection cleaning method.

According to Example 2a, a tubular reactor having a length of about 100 meters and an average inner diameter of about 41 cm, an L/D ratio of about 246, and 17 discharge ports distributed along the length was used. A drain cleaning method is used in which water is injected into the discharge line to help prevent gel accumulation in the discharge line.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time. The tubular reactor with an increased number of discharge ports has a smaller amount of steam traveling through the reaction tubes at each of the predetermined positions, and the steam in the tubes moves at a lower speed. The reduction in vapor volume and velocity allows less polymer mixture to travel into the discharge line, thereby allowing the discharge line to operate smoothly between cleaning times for a longer period of time. An increase in the number of discharge ports also helps prevent partial flashing of the liquid and embolic flow, thereby providing a more stable flow rate and a greater proportion of the annular flow.

Example 8b. Tubular reactor with longer length and finer diameter and increased number of discharge ports, using a water injection cleaning method.

According to Example 3, a tubular reactor having a length of about 100 meters and an average inner diameter of about 41 cm, an L/D ratio of about 246, and 17 discharge ports distributed along the length was used. A drain cleaning method is used in which water is injected into the discharge line to help prevent gel accumulation in the discharge line.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. Slowly heating the evaporated salt to make the polymer mixture less aerosolized, thereby allowing the cleaning between rows The pipeline is unobstructed for a long time. The tubular reactor with an increased number of discharge ports has a smaller amount of steam traveling through the reaction tubes at each of the predetermined positions, and the steam in the tubes moves at a lower speed. The reduction in vapor volume and velocity allows less polymer mixture to travel into the discharge line, thereby allowing the discharge line to operate smoothly between cleaning times for a longer period of time. An increase in the number of discharge ports also helps prevent partial flashing of the liquid and embolic flow, thereby providing a more stable flow rate and a greater proportion of the annular flow.

Example 8c. Tubular reactor with longer length and finer diameter and increased number of discharge ports, using a water injection cleaning method.

According to Example 2a, but with an average inner diameter of about 100 m and an average inner diameter of about 41 cm, a length of about 2.5 cm per 300 m, an inner diameter expansion ratio from the inlet end to the exit end, an L/D ratio of about 246, and a distribution along the length. A tubular reactor with 17 outlets. A drain cleaning method is used in which water is injected into the discharge line to help prevent gel accumulation in the discharge line.

Compared to Examples 1a-e and 2a-2b, when the evaporated salt mixture is heated to its target temperature, the tubular reactor heats the evaporated salt mixture more slowly, thereby allowing steam to be released from the reactor. Less improper by-products are formed and the loss of diamine is less. The slower heating of the evaporated salt causes the polymer mixture to be aerosolized less, thereby allowing the discharge line to pass between cleaning times for a longer period of time. The tubular reactor with an increased number of discharge ports has a smaller amount of steam traveling through the reaction tubes at each of the predetermined positions, and the steam in the tubes moves at a lower speed. The reduction in vapor volume and velocity allows less polymer mixture to travel into the discharge line, thereby allowing the discharge line to operate smoothly between cleaning times for a longer period of time. An increase in the number of discharge ports also helps prevent partial flashing of the liquid and embolic flow, thereby providing a more stable flow rate and a greater proportion of the annular flow. This increase in diameter reduces the generation and accumulation of gels and other impurities in the reactor, helping to maintain a larger proportion of the annular flow throughout the reactor. This rate of increase in diameter provides a pressure drop between the inlet and outlet of the reactor which allows for more efficient and efficient removal of water from the reactor, thereby reducing or preventing solidification of the polymer mixture in the reactor.

Example 9. Evaporator, tubular reactor and flasher heated via a secondary heating loop THERMINOL® 66 in the primary heating circuit, where there is a leak in the primary heating circuit.

Follow example 2a. A leak occurs in the primary heating circuit.

The liquid THERMINOL ^® 66 leaving the leak is at a relatively low pressure, limiting the total emissions of the material. Because the discharged liquid THERMINOL ^® 66 is relatively non-volatile, the risk of explosion is almost zero and the risk of ignition is low and limited to the point immediately adjacent to the leak.

Example 10. THERMINOL in a secondary heating loop with an evaporator heated by a secondary heating loop, a tubular reactor, and a flasher ^® 66, wherein there is a leak point in the secondary heating circuit.

Follow example 2a. A leak occurs in the secondary heating circuit of the tubular reactor.

Compared to Example 1d and 1e, the use of smaller volumes in the secondary heating circuit volatile DOWTHERM ^TM A pressurized high temperature will reduce the safety hazards associated with the flammable vapors. Compared to the one-stage heating circuit of Examples 1d and 1e, the smaller volume secondary heating circuit limits the amount of emissions that occur. Most of the heating systems in the plant operate continuously, while the secondary circuit containing DOWTHERM ^TM A shuts down to determine the point of leakage or extinguish the fire.

The use of the terms and expressions is intended to be illustrative and not limiting, and is not intended to be used as such terms and expressions, and any equivalents or portions thereof having the features shown and described are excluded. May be within the scope of the claimed creation. Modifications and variations of the concepts disclosed herein may be employed by those skilled in the art, and such modifications and variations are within the scope of the present invention as defined by the appended claims.

Other embodiments.

This creation provides at least the following, and its coding cannot be regarded as an indicative level of significance: Statement 1 provides a method of making polyamine, the method comprising: heating a first flowable heat transfer medium to provide a first heated Flowing heat transfer medium; and by the heated a flowable heat transfer medium transfers heat to the second flowable heat transfer medium to provide a heated second flowable heat transfer medium; and a tubular shape of the heated second flowable heat transfer medium to the polyamine synthesis system The reactor transfers heat.

Statement 2 provides the method of claim 1, wherein the tubular reactor comprises a length of from about 50 to about 300 meters.

The method of any one of statements 1 to 2, wherein the tubular reactor comprises a length of between about 75 and 125 meters.

The method of any one of statements 1 to 3, wherein the tubular reactor comprises an inner diameter of from about 10 cm to about 80 cm.

The method of any one of statements 1 to 4, wherein the tubular reactor comprises an inner diameter of from about 25 cm to about 60 cm.

The method of any one of statements 1 to 5, wherein the tubular reactor has a length/diameter (L/D) of from about 50 to about 2,500.

The method of any one of statements 1 to 6, wherein the tubular reactor has a length/diameter (L/D) of from about 100 to about 500.

The method of any one of statements 1 to 7, wherein the tubular reactor comprises a discharge port along its length.

Statement 9 provides the method of Statement 8, wherein the tubular reactor comprises from about 5 to about 50 discharge ports.

The method of any one of statements 8 to 9, wherein the tubular reactor comprises from about 10 to about 25 discharge ports.

The method of any one of statements 8 to 10, wherein the tubular reactor comprises an average of about 1 discharge port per about 3 meters to about 9 meters along the length of the tubular reactor.

The method of any one of statements 8 to 11, wherein the tubular reactor comprises an average of about 1 discharge port per about 2 meters to about 15 meters along the length of the tubular reactor.

The method of any one of statements 8 to 12, wherein the tubular reactor is along the The tubular reactor length comprises an average spacing of between about 2 meters and about 15 meters between the discharge ports.

The method of any one of statements 8 to 13, wherein the tubular reactor comprises an average spacing of between about 3 meters and about 9 meters between the discharge ports along the length of the tubular reactor.

The method of any one of statements 8 to 14, wherein the discharge ports are connected to a discharge line, the method comprising injecting water into the discharge lines.

The method of any one of statements 1 to 15, wherein the method is carried out for at least about 1 to about 5 years without the shutdown of the tubular reactor.

The method of any one of statements 1 to 16, wherein the method is carried out for at least about 2.5 to about 3 years without the shutdown of the tubular reactor.

The method of any one of statements 1 to 17, wherein the polyamine synthesis system synthesizes polyamine from a linear dicarboxylic acid and a linear diamine or an oligomer formed from a linear dicarboxylic acid and a linear diamine. .

The method of claim 18, wherein the dicarboxylic acid has the structure HOC(O)-R ¹ -C(O)OH, wherein R ¹ is a C ₁ -C ₁₅ alkylene group.

Statement 20 provides the method of claim 19, wherein the dicarboxylic acid is adipic acid.

The method of any one of statements 18 to 20, wherein the diamine has the structure H ₂ NR ² —NH ₂ , wherein R ² is a C ₁ -C ₁₅ alkylene group.

Statement 22 provides the method of claim 21, wherein the diamine is hexamethylenediamine.

The method of any one of statements 18 to 22, wherein the polyamine is nylon-6,6.

The method of any one of statements 1 to 23, wherein the first flowable heat transfer medium has a lower vapor pressure than the second flowable heat transfer medium at standard temperature and pressure.

The method of any one of statements 1 to 24, wherein the heated second flowable heat transfer medium has a higher vapor pressure than the heated first flowable heat transfer medium.

The method of any one of statements 1 to 25, wherein the heated second flowable heat transfer medium is more flammable and more flammable than the heated first flowable heat transfer medium. At least one of them.

The method of any one of statements 1 to 26, wherein the first flowable heat transfer medium comprises water, polyethylene glycol, polypropylene glycol, mineral oil, polyoxyphthalic acid, diphenyl ether, and biphenyl. At least one.

The method of any one of statements 1 to 27, wherein the first flowable heat transfer medium is at least one of: trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _{14 -30} alkyl aryl compound, diethyl benzene, vinylated benzene, cyclohexyl benzene, C _14-30 alkyl benzene, white petroleum mineral oil, ethyl diphenyl ethane, diphenyl ethane, diethyl di Ethylbenzene, diphenyl ether, diphenyl oxide, ethylbenzene polymer, biphenyl, inorganic salt, diisopropylbiphenyl, triisopropylbiphenyl, methylcyclohexane Alkane, bicyclohexane, terphenyl, hydrogenated terphenyl, partially hydrogenated p-tetraphenyl, partially hydrogenated high carbon polyphenyl, diphenyl ether, and phenanthrene, diaryl, triaryl, diaryl Alkyl ether, triaryl ether, alkylaryl compound, alkylaryl compound and diarylalkyl compound.

The method of any one of statements 1 to 28, wherein the heated first flowable heat transfer medium is from about 280 ° C to about 400 ° C.

The method of any one of statements 1 to 29, wherein the heated first flowable heat transfer medium is from about 330 °C to about 350 °C.

The method of any one of statements 1 to 30, wherein the first flowable heat transfer medium and the heated first flowable heat transfer medium are substantially liquid phases.

The method of any one of statements 1 to 31, wherein the first flowable heat transfer medium remains substantially liquid during heating of the first flowable heat transfer medium.

The method of any one of statements 1 to 32, wherein the first flowable heat transfer medium does not substantially vaporize during heating of the first flowable heat transfer medium.

The method of any one of statements 1 to 33, wherein the first flowable The heat transferred to the first flowable heat transfer medium during the transfer of the heat transfer medium comprises substantially all of the sensible heat.

The method of any one of statements 1 to 34, wherein the heated first flowable during the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat medium remains substantially liquid.

The method of any one of statements 1 to 35, wherein the heated first flowable during the transfer of the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat medium does not substantially condense.

The method of any one of statements 1 to 36, wherein the heated first flowable during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat transferred by the heat transfer medium contains substantially all of the sensible heat.

The method of any one of statements 1 to 37, wherein the first flowable heat transfer medium and the heated first flowable heat transfer medium are disposed in a first heating circuit.

The method of any one of statements 1 to 38, wherein the heated first flowable heat transfer medium provides heat to the second flowable heat transfer medium to provide a used first flowable heat transfer medium, It further includes a state in which the used first flowable heat transfer medium is circulated back to heat the first flowable heat transfer medium.

The method of any one of statements 1 to 39, wherein the second flowable heat transfer medium is water, polyethylene glycol, polypropylene glycol, mineral oil, polyoxygenated oil, diphenyl ether, biphenyl, and hydrazine At least one of triphenyls.

The method of any one of statements 1 to 40, wherein the second flowable heat transfer medium is at least one of: trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _{14 -30} alkyl aryl compound, diethyl benzene, vinylated benzene, cyclohexyl benzene, C _14-30 alkyl benzene, white petroleum mineral oil, ethyl diphenyl ethane, diphenyl ethane, diethyl di Ethylbenzene, diphenyl ether, diphenyl oxide, ethylbenzene polymer, biphenyl, inorganic salt, diisopropylbiphenyl, triisopropylbiphenyl, methylcyclohexane Alkane, bicyclohexane, terphenyl, hydrogenated terphenyl, partially hydrogenated p-tetraphenyl, partially hydrogenated high carbon polyphenyl, diphenyl ether, and phenanthrene, diaryl, triaryl, diaryl Alkyl ether, triaryl ether, alkylaryl compound, alkylaryl compound and diarylalkyl compound.

The method of any one of statements 1 to 41, wherein the heated first flowable heat transfer medium is from about 210 °C to about 350 °C.

The method of any one of statements 1 to 42, wherein the heated first flowable heat transfer medium is from about 260 ° C to about 300 ° C.

The method of any one of statements 1 to 43 wherein the heated second flowable heat transfer medium is a substantially liquid phase.

The method of any one of statements 1 to 44, wherein the heated second flowable heat transfer medium is substantially gaseous.

The method of any one of statements 1 to 45, wherein the second flowable heat transfer medium is substantially during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium It turns into a gas.

The method of any one of statements 1 to 46, wherein the second flowable heat transfer medium is substantially during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium All vaporized.

Statement 48 provides the method of statement 47, further comprising controlling a pressure of the second flowable heat transfer medium to control a temperature at which the second flowable heat transfer medium vaporizes.

The method of claim 48, wherein the second heat transfer medium and the heated second heat transfer medium are disposed in a second heating circuit, wherein controlling the pressure of the second flowable heat transfer medium comprises controlling the The pressure in the heating circuit.

The method of any one of statements 48 to 49, wherein the temperature at which the second flowable heat transfer medium is vaporized is controlled to control the temperature of the tubular reactor.

The method of any one of statements 1 to 50, wherein the second flowable during the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat transferred by the hydrothermal medium contains substantially all of the latent heat, which contains heat of vaporization.

The method of any one of statements 1 to 51, wherein the second flowable heat transfer medium is transferred during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat transferred contains about 70-100% latent heat and about 0 to 30% sensible heat, which contains heat of vaporization.

The method of any one of statements 1 to 52, wherein during the heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system, the heated second The flowable heat transfer medium is substantially condensed into a liquid.

Statement 54 provides the method of claim 53, further comprising controlling a pressure of the heated second flowable heat transfer medium to adjust a temperature at which the heated second flowable heat transfer medium undergoes at least partial condensation.

Statement 55 provides the method of statement 54, wherein controlling the temperature at which the heated second flowable heat transfer medium undergoes at least partial condensation controls the temperature of the tubular reactor.

The method of any one of statements 54 to 55, wherein the second heat transfer medium and the heated second heat transfer medium are disposed in a second heating circuit, wherein the heated second flowable medium is controlled The pressure of the heat medium includes controlling the pressure in the second heating circuit.

Statement 57 provides the method of statement 56, wherein controlling the pressure in the second heating circuit comprises controlling a saturation temperature of the heated second flowable heat transfer medium.

Statement 58 provides the method of claim 57, wherein a maximum temperature of the heated second flowable heat transfer medium differs from the saturated temperature of the heated second flowable heat transfer medium by between about 0 °C and 40 °C.

The method of any one of statements 1 to 58, wherein the heated second flowable heat transfer medium is transferred during heat transfer from the heated second flowable heat transfer medium to the tubular reactor This heat contains substantially all latent heat, which contains heat of vaporization.

The statement 60 provides the method of any one of statements 1 to 59, wherein During the heat transfer of the two flowable heat transfer medium to the tubular reactor, the heat transferred by the second flowable heat transfer medium comprises about 70-100% latent heat and about 0-30% sensible heat, the latent heat comprising heat of vaporization.

The method of any one of statements 1 to 60, wherein the heated second flowable heat transfer medium provides heat to the tubular reactor to provide a used second flowable heat transfer medium, further comprising The used second flowable heat transfer medium is circulated back to the state of heat transfer by the heated first flowable heat transfer medium.

The method of any one of statements 1 to 61, wherein the transferring the heated second flowable heat transfer medium to the tubular reactor comprises maintaining the temperature of the tubular reactor at about 150 ° C to about 350 ° C.

The method of any one of statements 1 to 62, wherein the transferring the heated second flowable heat transfer medium to the tubular reactor comprises maintaining the temperature of the tubular reactor at about 210 ° C to about 260 ° C.

The method of any one of statements 1 to 63, wherein the transferring the heated second flowable heat transfer medium to the tubular reactor comprises maintaining the temperature of the polyamidamide mixture in the reactor at about 218 °C to about 250 °C.

The method of any one of statements 1 to 64, wherein the heated first flowable heat transfer medium provides heat to the second flowable heat transfer medium to provide a used first flowable heat transfer medium, The method further includes transferring heat from the used first flowable heat transfer medium or from the heated first flowable heat transfer medium to the third flowable heat transfer medium to provide a heated third flowable heat transfer a medium; transferring heat from the heated third flowable heat transfer medium to at least one polyamine-containing component of the polyamide synthesis system.

Statement 66 provides the method of claim 65, wherein the at least one component of the polyamine synthesis system that is heat transferred by the heated third flowable heat transfer medium is different from the tubular reactor.

Statement 67 provides a method of making nylon-6,6 comprising: heating comprising terphenyl a first flowable heat transfer medium providing a heated first flowable heat transfer medium; passing the heated first flowable heat transfer medium comprising diphenyl ether and biphenyl to the second flowable heat transfer medium Heating, providing a heated second flowable heat transfer medium and a used first flowable heat transfer medium, wherein the first flowable heat transfer medium, the heated first flowable heat transfer medium, and the used The first flowable heat transfer medium is disposed in the first heating circuit, and heats the first flowable heat transfer medium and transfers heat from the heated first flowable heat transfer medium to the second flowable heat transfer medium The first flowable heat transfer medium, the heated first flowable heat transfer medium, and the used first flowable heat transfer medium are substantially liquid phase, and are delivered to the first flowable heat transfer medium The heat and the heat transferred by the first flowable heat transfer medium comprise substantially all sensible heat, and during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium, The second flowable heat transfer medium is substantially completely vaporized; The first flowable heat transfer medium is circulated back to heat the state of the first flowable heat transfer medium; the heated second flowable heat transfer medium transfers heat to the tubular reactor of the polyamide synthesis system to provide used a second flowable heat transfer medium, wherein the second flowable heat transfer medium and the heated second flowable heat transfer medium are disposed in a second heating circuit, the second flowable heat transfer medium and the used The second flowable heat transfer medium is a substantially liquid phase, the heated second flowable heat transfer medium is a substantially liquid phase, and the heat transferred to the second flowable heat transfer medium and the second The heat transferred by the flowing heat transfer medium comprises about 70-100% latent heat and about 0-30% sensible heat, the latent heat including heat of vaporization; controlling the pressure of the second heat transfer loop to control saturation of the second flowable heat transfer medium Temperature, wherein the saturation temperature is controlled to control the temperature of the tubular reactor; and circulating the used second flowable heat transfer medium back to a state of heat transfer from the heated first flowable heat transfer medium; The tubular reactor contains from about 75 to about 125 meters In length, the tubular reactor comprises an inner diameter of from about 25 centimeters to about 60 centimeters, the tubular reactor comprises a length/diameter (L/D) of from about 100 to about 500, and wherein the tubular reactor comprises about 10 along its length. Up to about 25 discharges.

Statement 68 provides a method of making polyamine, the method comprising: heating a first flowable a heat transfer medium to provide a heated first flowable heat transfer medium; and to transfer heat from the heated first flowable heat transfer medium to the second flowable heat transfer medium to provide a heated second flowable heat transfer And transferring, by the heated second flowable heat transfer medium, to a tubular reactor of the polyamine synthesis system; wherein the tubular reactor comprises a length of from about 75 to about 125 meters, the tubular reactor comprising about From 25 centimeters to about 60 centimeters, the tubular reactor comprises from about 100 to about 500 lengths/diameter (L/D), and wherein the tubular reactor comprises from about 10 to about 25 discharge ports along its length.

Statement 69 provides a system for making polyamine, the system comprising: a heater configured to heat a first flowable heat transfer medium to provide a heated first flowable heat transfer medium; a first heat exchanger Configuring to transfer heat from the heated first flowable heat transfer medium to provide a heated second flowable heat transfer medium; and a second heat exchanger configured to be heated by the second The flowable heat transfer medium transfers heat to the tubular reactor of the polyamine synthesis system.

Statement 70 provides a device for making polyamine, the device comprising: a heater configured to heat a first flowable heat transfer medium to provide a heated first flowable heat transfer medium; a first heat exchanger Configuring to transfer heat from the heated first flowable heat transfer medium to provide a heated second flowable heat transfer medium; and a second heat exchanger configured to be heated by the second The flowable heat transfer medium transfers heat to the tubular reactor of the polyamine synthesis unit.

Statement 71 provides the apparatus of claim 70, wherein the tubular reactor comprises a length of from about 50 to about 300 meters.

The device of any one of statements 70 to 71, wherein the tubular reactor comprises a length of between about 75 and 125 meters.

The device of any one of statements 70 to 72, wherein the tubular reactor comprises an inner diameter of from about 10 cm to about 80 cm.

The invention provides the apparatus of any one of statements 70 to 73, wherein the tubular reactor package It has an inner diameter of from about 25 cm to about 60 cm.

The apparatus of any one of statements 70 to 74, wherein the tubular reactor has a length/diameter (L/D) of from about 50 to about 2,500.

The apparatus of any one of statements 70 to 75, wherein the tubular reactor has a length/diameter (L/D) of from about 100 to about 500.

The device of any one of statements 70 to 76, wherein the tubular reactor comprises a discharge port along its length.

Statement 78 provides the apparatus of claim 77, wherein the tubular reactor comprises from about 5 to about 50 discharge ports.

The apparatus of any one of statements 77 to 78, wherein the tubular reactor comprises from about 10 to about 25 discharge ports.

The apparatus of any one of statements 77 to 79, wherein the tubular reactor comprises an average of about 1 discharge port per about 3 meters to about 9 meters along the length of the tubular reactor.

The apparatus of any one of statements 77 to 80, wherein the tubular reactor comprises, on the length of the tubular reactor, an average of about 1 discharge port per about 2 meters to about 15 meters.

The apparatus of any one of statements 77 to 81, wherein the tubular reactor comprises an average spacing of between about 2 meters and about 15 meters between the discharge ports along the length of the tubular reactor.

The apparatus of any one of statements 77 to 82, wherein the tubular reactor comprises an average spacing of between about 3 meters and about 9 meters between the discharge ports along the length of the tubular reactor.

The statement 84 provides the device of any one of statements 77 to 83, wherein the discharge ports are connected to a discharge line, the device comprising injecting water into the discharge lines.

Statement 85 provides the apparatus of any one of statements 70 to 84, wherein the method is carried out for at least about 1 to about 5 years without the tubular reactor being cleaned.

Statement 86 provides the apparatus of any one of statements 70 to 85, wherein the method is in the tubular inverse The device is allowed to be cleaned for at least about 2.5 to about 3 years without stopping.

The device of any one of statements 70 to 86, wherein the device for producing the polyamine is configured to be oligomerized from a linear dicarboxylic acid and a linear diamine or from a linear dicarboxylic acid and a linear diamine. The polyamine is synthesized.

Statement 88 provides the apparatus of claim 87, wherein the dicarboxylic acid has the structure HOC(O)-R ¹ -C(O)OH, wherein R ¹ is a C ₁ -C ₁₅ alkylene group.

Statement 89 provides the device of claim 88, wherein the dicarboxylic acid is adipic acid.

The apparatus of any one of statements 87 to 89, wherein the diamine has the structure H ₂ NR ² —NH ₂ , wherein R ² is a C ₁ -C ₁₅ alkylene group.

Statement 91 provides the apparatus of claim 90, wherein the diamine is hexamethylenediamine.

The device of any one of statements 87 to 91, wherein the polyamine is nylon-6,6.

The apparatus of any one of statements 70 to 92, wherein the first flowable heat transfer medium has a lower vapor pressure than the second flowable heat transfer medium at a standard temperature and pressure.

The apparatus of any one of statements 70 to 93, wherein the heated second flowable heat transfer medium has a higher vapor pressure than the heated first flowable heat transfer medium.

The device of any one of statements 70 to 94, wherein the heated second flowable heat transfer medium is more flammable and more flammable than the heated first flowable heat transfer medium At least one of them.

The apparatus of any one of statements 70 to 95, wherein the first flowable heat transfer medium comprises water, polyethylene glycol, polypropylene glycol, mineral oil, polyoxyphthalic acid, diphenyl ether, and biphenyl. At least one.

The apparatus of any one of statements 70 to 96, wherein the first flowable heat transfer medium is at least one of: trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _{14 -30} alkyl aryl compound, diethyl benzene, vinylated benzene, cyclohexyl benzene, C _14-30 alkyl benzene, white petroleum mineral oil, ethyl diphenyl ethane, diphenyl ethane, diethyl di Ethylbenzene, diphenyl ether, diphenyl oxide, ethylbenzene polymer, biphenyl, inorganic salt, diisopropylbiphenyl, triisopropylbiphenyl, methylcyclohexane Alkane, bicyclohexane, terphenyl, hydrogenated terphenyl, partially hydrogenated p-tetraphenyl, partially hydrogenated high carbon polyphenyl, diphenyl ether, and phenanthrene, diaryl, triaryl, diaryl Alkyl ether, triaryl ether, alkylaryl compound, alkylaryl compound and diarylalkyl compound.

The device of any one of statements 70 to 97, wherein the heated first flowable heat transfer medium is between about 280 ° C and about 400 ° C.

The device of any one of statements 70 to 98, wherein the heated first flowable heat transfer medium is from about 330 °C to about 350 °C.

The device of any one of statements 70 to 99, wherein the first flowable heat transfer medium and the heated first flowable heat transfer medium are substantially liquid phase.

The apparatus of any one of statements 70 to 100, wherein the first flowable heat transfer medium remains substantially liquid during heating of the first flowable heat transfer medium.

The statement 102 provides the apparatus of any one of statements 70 to 101, wherein the first flowable heat transfer medium does not substantially vaporize during heating of the first flowable heat transfer medium.

The statement 103 provides the apparatus of any one of statements 70 to 102, wherein the heat transferred to the first flowable heat transfer medium during heating of the first flowable heat transfer medium comprises substantially all sensible heat.

The apparatus of any one of statements 70 to 103, wherein the heated first flowable during the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat medium remains substantially liquid.

The apparatus of any one of statements 70 to 104, wherein the heated during the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The first flowable heat transfer medium does not substantially condense.

The apparatus of any one of statements 70 to 105, wherein the heated first flowable during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat transferred by the heat transfer medium contains substantially all of the sensible heat.

The apparatus of any one of statements 70 to 106, wherein the first flowable heat transfer medium and the heated first flowable heat transfer medium are disposed in a first heating circuit.

The apparatus of any one of statements 70 to 107, wherein the heated first flowable heat transfer medium provides heat to the second flowable heat transfer medium to provide a used first flowable heat transfer medium, It further includes a state in which the used first flowable heat transfer medium is circulated back to heat the first flowable heat transfer medium.

The apparatus of any one of statements 70 to 108, wherein the second flowable heat transfer medium is water, polyethylene glycol, polypropylene glycol, mineral oil, polyoxygenated oil, diphenyl ether, biphenyl, and hydrazine At least one of triphenyls.

The apparatus of any one of statements 70 to 109, wherein the second flowable heat transfer medium is at least one of: trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _{14 -30} alkyl aryl compound, diethyl benzene, vinylated benzene, cyclohexyl benzene, C _14-30 alkyl benzene, white petroleum mineral oil, ethyl diphenyl ethane, diphenyl ethane, diethyl di Ethylbenzene, diphenyl ether, diphenyl oxide, ethylbenzene polymer, biphenyl, inorganic salt, diisopropylbiphenyl, triisopropylbiphenyl, methylcyclohexane Alkane, bicyclohexane, terphenyl, hydrogenated terphenyl, partially hydrogenated p-tetraphenyl, partially hydrogenated high carbon polyphenyl, diphenyl ether, and phenanthrene, diaryl, triaryl, diaryl Alkyl ether, triaryl ether, alkylaryl compound, alkylaryl compound and diarylalkyl compound.

The apparatus of any one of statements 70 to 110, wherein the heated second flowable heat transfer medium is from about 210 ° C to about 350 ° C.

The statement 112 provides the apparatus of any one of statements 70 to 111, wherein the heated second The flowable heat transfer medium is from about 260 ° C to about 300 ° C.

The apparatus of any one of statements 70 to 112, wherein the heated second flowable heat transfer medium is a substantially liquid phase.

The apparatus of any one of statements 70 to 113, wherein the heated second flowable heat transfer medium is substantially vapor phase.

The apparatus of any one of statements 70 to 114, wherein the second flowable heat transfer medium is substantially during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium It turns into a gas.

The apparatus of any one of statements 70 to 115, wherein the second flowable heat transfer medium is substantially during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium All vaporized.

The invention of claim 117, wherein the second heat transfer medium and the heated second heat transfer medium are disposed in the second heating circuit.

Statement 118 provides the apparatus of claim 117, wherein the second heating circuit is configured to control the pressure of the second flowable heat transfer medium to control the temperature at which the second flowable heat transfer medium vaporizes.

Statement 119 provides a device for statement 118 in which the temperature at which the second flowable heat transfer medium is vaporized is controlled to control the temperature of the tubular reactor.

The apparatus of any one of statements 70 to 119, wherein the second flowable heat transfer medium is transferred during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat transferred contains substantially all latent heat, which contains heat of vaporization.

The apparatus of any one of statements 70 to 120, wherein the second flowable heat transfer medium is transferred during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium The heat transferred contains about 70-100% latent heat and about 0-30% sensible heat, which contains heat of vaporization.

The statement 122 provides the device of any one of statements 70 to 121, wherein During heating of the second flowable heat transfer medium to the tubular reactor, the heated second flowable heat transfer medium is substantially condensed into a liquid.

Statement 123 provides the apparatus of statement 122, further comprising a controller configured to control the pressure of the heated second flowable heat transfer medium to adjust the heated second flowable heat transfer medium to undergo at least partial condensation The temperature.

Statement 124 provides the apparatus of claim 123 wherein the temperature at which the heated second flowable heat transfer medium undergoes at least partial condensation is controlled to control the temperature of the tubular reactor.

The apparatus of any one of statements 123 to 124, wherein the second heat transfer medium and the heated second heat transfer medium are disposed in a second heating circuit, wherein the heated second flowable medium is controlled The pressure of the heat medium includes controlling the pressure in the second heating circuit.

Statement 126 provides the apparatus of statement 125 wherein controlling the pressure in the second heating circuit comprises controlling a saturation temperature of the heated second flowable heat transfer medium.

Statement 127 provides the apparatus of claim 126, wherein the highest temperature of the heated second flowable heat transfer medium differs from the saturation temperature of the heated second flowable heat transfer medium by between about 0 °C and 40 °C.

The apparatus of any one of statements 70 to 127, wherein the heated second flowable heat transfer medium is transferred during heat transfer from the heated second flowable heat transfer medium to the tubular reactor This heat contains substantially all latent heat, which contains heat of vaporization.

The apparatus of any one of statements 70 to 128, wherein the heat transferred by the second flowable heat transfer medium during heat transfer from the heated second flowable heat transfer medium to the tubular reactor comprises About 70-100% latent heat and about 0-30% sensible heat, which contains heat of vaporization.

The statement 130 provides the apparatus of any one of statements 70 to 129, wherein the heated second flowable heat transfer medium provides heat transfer to the tubular reactor of the polyamide synthesis system And passing over the second flowable heat transfer medium, further comprising recycling the used second flowable heat transfer medium to a state of heat transfer from the heated first flowable heat transfer medium.

The apparatus of any one of statements 70 to 130, wherein the heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system comprises the polyamine synthesis system The temperature of the tubular reactor is maintained between about 150 ° C and about 350 ° C.

The apparatus of any one of statements 70 to 131, wherein the heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamine synthesis system comprises the polyamine synthesis system The temperature of the tubular reactor is maintained between about 210 ° C and about 260 ° C.

The 133. The apparatus of any one of statements 70 to 132, wherein the heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system comprises mixing the polyamine mixture in the reactor The temperature is maintained between about 218 ° C and about 250 ° C.

The device of any one of statements 70 to 133, wherein the heated first flowable heat transfer medium provides heat to the second flowable heat transfer medium to provide a used first flowable heat transfer medium, Wherein the second heat exchanger is configured to transfer heat from the used first flowable heat transfer medium or from the heated first flowable heat transfer medium to the third flowable heat transfer medium to provide a third flowable heat transfer medium that is heated, the apparatus further comprising a third heat exchanger configured to pass at least one of the heated third flowable heat transfer medium to the polyamine synthesis system Heat transfer of the amine component, the polyamine synthesis system comprising at least one of a preheater, an evaporator, a polymerization reactor, a flasher, a finishing machine, and an autoclave.

Statement 135 provides the apparatus of claim 134, wherein the at least one component of the polyamine synthesis system that is heat transferred by the heated third flowable heat transfer medium is different from the tubular reactor.

Statement 136 provides a device for making nylon-6,6, the device comprising: a heater configured to heat a first flowable heat transfer medium comprising terphenyl to provide a first heated a flow heat transfer medium; a first heat exchanger configured to transfer heat from the heated first flowable heat transfer medium to a second flowable heat transfer medium comprising diphenyl ether and biphenyl to provide Heating the second flowable heat transfer medium and the used first flowable heat transfer medium, and circulating the used first flowable heat transfer medium back to the first heat exchanger, wherein the first flowable The heat transfer medium, the heated first flowable heat transfer medium, and the used first flowable heat transfer medium are disposed in the first heating circuit, heating the first flowable heat transfer medium and heating the first flowable heat transfer medium During the heat transfer of the first flowable heat transfer medium to the second flowable heat transfer medium, the first flowable heat transfer medium, the heated first flowable heat transfer medium, and the used first flowable The heat transfer medium is a substantially liquid phase, the heat transferred to the first flowable heat transfer medium and the heat transferred by the first flowable heat transfer medium comprise substantially all sensible heat, and by the heated Heat transfer of the first flowable heat transfer medium to the second flowable heat transfer medium The second flowable heat transfer medium is substantially completely vaporized; and a second heat exchanger configured to transfer heat from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system, Providing a used second flowable heat transfer medium and circulating the used second flowable heat transfer medium back to a state of heat transfer from the heated first flowable heat transfer medium, wherein the second flowable The heat transfer medium and the heated second flowable heat transfer medium are disposed in a second heating circuit, the second heating circuit configured to control a pressure of the second heat transfer loop to control the second flowable heat transfer a saturation temperature of the medium, wherein the saturation temperature is controlled to control the temperature of the tubular reactor, the second flowable heat transfer medium and the used second flowable heat transfer medium are substantially liquid phase, the heated first The second flowable heat transfer medium is substantially liquid phase, and the heat transferred to the second flowable heat transfer medium and the heat transferred by the second flowable heat transfer medium comprise about 70-100% latent heat and about 0-30 % sensible heat, the latent heat containing heat of vaporization; wherein the tube The reactor comprises a length of from about 75 to about 125 meters, the tubular reactor comprises an inner diameter of from about 25 centimeters to about 60 centimeters, and the tubular reactor comprises a length/diameter (L/D) of from about 100 to about 500, and Wherein the tubular reactor comprises from about 10 to about 25 discharge ports along its length.

Statement 137 provides an apparatus or method of any one or any combination of statements 1 to 136, which is optionally configured such that all of the described elements or options are available.

10‧‧‧Systems or devices for the manufacture of polyamines

15‧‧‧heater

20‧‧‧First flowable heat transfer medium

25‧‧‧First heating circuit

30‧‧‧The first flowable heat transfer medium heated

35‧‧‧First heat exchanger

40‧‧‧Second flowable heat transfer medium

45‧‧‧Secondary heating circuit

50‧‧‧heated second flowable heat transfer medium

55‧‧‧second heat exchanger

Claims (68)

A device for producing polyamine, the device comprising: a heater configured to heat a first flowable heat transfer medium to provide a heated first flowable heat transfer medium; a first heat exchanger, the group of which is And providing a heated second flowable heat transfer medium by transferring the heated first flowable heat transfer medium to the second flowable heat transfer medium; and a second heat exchanger configured to be The heated second flowable heat transfer medium transfers heat to the tubular reactor of the polyamine synthesis system. A device for producing polyamine, the device comprising: a heater configured to heat a first flowable heat transfer medium to provide a heated first flowable heat transfer medium; a first heat exchanger, the group of which is a second flowable heat transfer medium that is heated by the heated first flowable heat transfer medium; and a second heat exchanger configured to be flowable by the heated second flow The heat transfer medium transfers heat to the tubular reactor of the polyamine synthesis system. The device of claim 1 wherein the tubular reactor comprises a length of from 50 to 300 meters. The device of claim 1, wherein the tubular reactor comprises a length of from 75 to 125 meters. The device of claim 1, wherein the tubular reactor comprises an inner diameter of from 10 cm to 80 cm. The device of claim 1, wherein the tubular reactor comprises an inner diameter of from 25 cm to 60 cm. The apparatus of claim 1, wherein the tubular reactor has a length/diameter (L/D) of 50 to 2500. The apparatus of claim 1, wherein the tubular reactor has a length/diameter (L/D) of from 100 to 500. The device of claim 1, wherein the tubular reactor comprises a discharge port along its length. The device of claim 9, wherein the tubular reactor comprises from 5 to 50 discharge ports. The device of claim 9, wherein the tubular reactor comprises from 10 to 25 discharge ports. The apparatus of claim 9, wherein the tubular reactor comprises an average of one discharge port per 3 meters to 9 meters along the length of the tubular reactor. The apparatus of claim 9, wherein the tubular reactor comprises an average of one discharge port per 2 meters to 15 meters along the length of the tubular reactor. The apparatus of claim 9, wherein the tubular reactor comprises an average spacing between 2 and 15 meters between the discharge ports along the length of the tubular reactor. The apparatus of claim 9, wherein the tubular reactor comprises an average spacing of between 3 and 9 meters between the discharge ports along the length of the tubular reactor. The apparatus of claim 9, wherein the discharge ports are connected to a discharge line, the apparatus comprising injecting water into the discharge lines. The apparatus of claim 1, wherein the apparatus is operated for at least 1 to 5 years without the tubular reactor being cleaned. The apparatus of claim 1, wherein the apparatus is operated for at least 2.5 to 3 years without the tubular reactor being cleaned. The device of claim 1, wherein the device for producing the polyamine is configured to synthesize the polyamine from a linear dicarboxylic acid and a linear diamine or an oligomer formed from a linear dicarboxylic acid and a linear diamine. . The device of claim 19, wherein the dicarboxylic acid has the structure HOC(O)-R ¹ -C(O)OH, wherein R ¹ is a C ₁ -C ₁₅ alkylene group. The device of claim 20, wherein the dicarboxylic acid is adipic acid. The device of claim 19, wherein the diamine has the structure H ₂ NR ² —NH ₂ , wherein R ² is a C ₁ -C ₁₅ alkylene group. The device of claim 22, wherein the diamine is hexamethylenediamine. The device of claim 19, wherein the polyamine is nylon-6,6. The apparatus of claim 1 wherein the first flowable heat transfer medium has a lower vapor pressure than the second flowable heat transfer medium at standard temperature and pressure. The apparatus of claim 1 wherein the heated second flowable heat transfer medium has a higher vapor pressure than the heated first flowable heat transfer medium. The apparatus of claim 1 wherein the heated second flowable heat transfer medium is at least one of more flammable and more combustible than the heated first flowable heat transfer medium. The device of claim 1, wherein the first flowable heat transfer medium comprises at least one of water, polyethylene glycol, polypropylene glycol, mineral oil, polyoxyxane, diphenyl ether, and biphenyl. The apparatus of claim 1, wherein the first flowable heat transfer medium is at least one of: trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _14-30 alkyl aryl compound , diethylbenzene, vinylated benzene, cyclohexylbenzene, C _14-30 alkylbenzene, white petroleum mineral oil, ethyl diphenylethane, diphenylethane, diethyldiphenylethane, diphenyl ether (diphenyl ether), diphenyl oxide, ethylbenzene polymer, biphenyl, inorganic salt, diisopropylbiphenyl, triisopropylbiphenyl, methylcyclohexane, dicyclohexyl, Biphenyl, hydrogenated terphenyl, partially hydrogenated biphenyl, partially hydrogenated high carbon polyphenyl, diphenyl ether, and phenanthrene, diaryl, triaryl, diaryl ether, triaryl ether, An alkylaryl compound, an alkylaryl compound, and a diarylalkyl compound. The apparatus of claim 1 wherein the heated first flowable heat transfer medium is between 280 ° C and 400 ° C. The device of claim 1, wherein the heated first flowable heat transfer medium is 330 ° C Up to 350 ° C. The device of claim 1, wherein the first flowable heat transfer medium and the heated first flowable heat transfer medium are substantially liquid phase. The device of claim 1 wherein the first flowable heat transfer medium remains substantially liquid during heating of the first flowable heat transfer medium. The apparatus of claim 1 wherein the first flowable heat transfer medium does not substantially vaporize during heating of the first flowable heat transfer medium. The apparatus of claim 1 wherein the heat transferred to the first flowable heat transfer medium during the heating of the first flowable heat transfer medium comprises substantially all of the sensible heat. The apparatus of claim 1 wherein the heated first flowable heat transfer medium remains substantially liquid during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium . The apparatus of claim 1, wherein the heated first flowable heat transfer medium does not substantially condense during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium . The apparatus of claim 1 wherein the heat transferred by the heated first flowable heat transfer medium during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium Contains virtually all sensible heat. The apparatus of claim 1, wherein the first flowable heat transfer medium and the heated first flowable heat transfer medium are disposed in the first heating circuit. The apparatus of claim 1, wherein the heated first flowable heat transfer medium provides heat to the second flowable heat transfer medium to provide a used first flowable heat transfer medium, further comprising using the used The first flowable heat transfer medium circulates back to the state of heating the first flowable heat transfer medium. The device of claim 1, wherein the second flowable heat transfer medium is water, polyethylene glycol, polypropylene glycol, mineral oil, polyoxygenated oil, diphenyl ether, biphenyl and terphenyl. At least one of them. The device of claim 1, wherein the second flowable heat transfer medium is at least one of: trimethylpentane, C _10-13 alkane, C _10-13 isoalkane, C _14-30 alkyl aryl compound , diethylbenzene, vinylated benzene, cyclohexylbenzene, C _14-30 alkylbenzene, white petroleum mineral oil, ethyl diphenylethane, diphenylethane, diethyldiphenylethane, diphenyl ether (diphenyl ether), diphenyl oxide, ethylbenzene polymer, biphenyl, inorganic salt, diisopropylbiphenyl, triisopropylbiphenyl, methylcyclohexane, dicyclohexyl, Biphenyl, hydrogenated terphenyl, partially hydrogenated biphenyl, partially hydrogenated high carbon polyphenyl, diphenyl ether, and phenanthrene, diaryl, triaryl, diaryl ether, triaryl ether, An alkylaryl compound, an alkylaryl compound, and a diarylalkyl compound. The apparatus of claim 1 wherein the heated second flowable heat transfer medium is between 210 ° C and 350 ° C. The apparatus of claim 1 wherein the heated second flowable heat transfer medium is between 260 ° C and 300 ° C. The device of claim 1 wherein the heated second flowable heat transfer medium is a substantially liquid phase. The apparatus of claim 1 wherein the heated second flowable heat transfer medium is substantially vapor phase. The apparatus of claim 1 wherein the second flowable heat transfer medium substantially becomes a gas during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium. The apparatus of claim 1 wherein the second flowable heat transfer medium is substantially completely vaporized during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium. The device of claim 1, wherein the second flowable heat transfer medium and the heated first The two flowable heat transfer medium is disposed in the second heating circuit. The apparatus of claim 49, wherein the second heating circuit is configured to control the pressure of the second flowable heat transfer medium to control the temperature at which the second flowable heat transfer medium vaporizes. The apparatus of claim 50, wherein the temperature controlling the vaporization of the second flowable heat transfer medium controls the temperature of the tubular reactor. The apparatus of claim 1, wherein the heat transferred to the second flowable heat transfer medium during the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium comprises substantially All latent heat, which contains heat of vaporization. The apparatus of claim 1 wherein during the heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium, the heat transferred to the second flowable heat transfer medium comprises 70- 100% latent heat and 0-30% sensible heat, which contains heat of vaporization. The apparatus of claim 1 wherein the heated second flowable heat transfer medium substantially condenses into a liquid during heat transfer from the heated second flowable heat transfer medium to the tubular reactor. The apparatus of claim 54, further comprising a controller configured to control a pressure of the heated second flowable heat transfer medium to adjust the heated second flowable heat transfer medium to undergo at least partial condensation temperature. The apparatus of claim 55, wherein controlling the temperature at which the heated second flowable heat transfer medium undergoes at least partial condensation controls the temperature of the tubular reactor. The apparatus of claim 55, wherein the second flowable heat transfer medium and the heated second flowable heat transfer medium are disposed in a second heating circuit, wherein the heated second flowable heat transfer medium is controlled The pressure includes controlling the pressure in the second heating circuit. The apparatus of claim 57, wherein controlling the pressure in the second heating circuit comprises The saturation temperature of the heated second flowable heat transfer medium is controlled. The apparatus of claim 58, wherein the highest temperature of the heated second flowable heat transfer medium is within 0 ° C to 40 ° C of the saturated temperature of the heated second flowable heat transfer medium. The apparatus of claim 1 wherein during the transfer of heat from the heated second flowable heat transfer medium to the tubular reactor, the heat transferred by the heated second flowable heat transfer medium comprises substantially all Latent heat, which contains heat of vaporization. The apparatus of claim 1, wherein the heat transferred by the heated second flowable heat transfer medium comprises 70-100 during heat transfer from the heated second flowable heat transfer medium to the tubular reactor % latent heat and 0-30% sensible heat, which contains heat of vaporization. The apparatus of claim 1 wherein the heated second flowable heat transfer medium provides heat to the tubular reactor of the polyamide synthesis system to provide a used second flowable heat transfer medium, further comprising The used second flowable heat transfer medium is circulated back to the state of heat transfer by the heated first flowable heat transfer medium. The apparatus of claim 1, wherein the heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system comprises the temperature of the tubular reactor of the polyamine synthesis system Maintained at 150 ° C to 350 ° C. The apparatus of claim 1, wherein the heat transfer from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system comprises the temperature of the tubular reactor of the polyamine synthesis system Maintained at 210 ° C to 260 ° C. The apparatus of claim 1 wherein the transferring of the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system comprises maintaining a temperature of the polyamine mixture in the tubular reactor at 218 ° C to 250 ° C. The apparatus of claim 1 wherein the heated first flowable heat transfer medium provides heat to the second flowable heat transfer medium to provide a used first flowable heat transfer medium, The second heat exchanger is configured to provide heat transfer from the used first flowable heat transfer medium or from the heated first flowable heat transfer medium to the third flowable heat transfer medium a heated third flowable heat transfer medium, the apparatus further comprising a third heat exchanger configured to contain at least one of the heated third flowable heat transfer medium to the polyamine synthesis system The heat transfer of the guanamine assembly comprises at least one of a preheater, an evaporator, a polymerization reactor, a flasher, a finishing machine, and an autoclave. The apparatus of claim 66, wherein the at least one component of the polyamine synthesis system that is heat transferred by the heated third flowable heat transfer medium is different from the tubular reactor. A device for making nylon-6,6, the device comprising: a heater configured to heat a first flowable heat transfer medium comprising biphenyl to provide a heated first flowable heat transfer medium; a heat exchanger configured to transfer heat from the heated first flowable heat transfer medium to a second flowable heat transfer medium comprising diphenyl ether and biphenyl to provide a heated second flowable a heat medium and a used first flowable heat transfer medium, and circulating the used first flowable heat transfer medium back to the first heat exchanger, wherein the first flowable heat transfer medium, the heated The first flowable heat transfer medium and the used first flowable heat transfer medium are disposed in the first heating circuit, heating the first flowable heat transfer medium and being heated by the first flowable medium During the heat transfer of the heat medium to the second flowable heat transfer medium, the first flowable heat transfer medium, the heated first flowable heat transfer medium, and the used first flowable heat transfer medium are substantially a liquid phase, the heat transferred to the first flowable heat transfer medium and by the first The heat transferred by the flowing heat transfer medium comprises substantially all of the sensible heat, and The second flowable heat transfer medium is substantially completely vaporized during heat transfer from the heated first flowable heat transfer medium to the second flowable heat transfer medium; and the second heat exchanger is configured Transferring heat from the heated second flowable heat transfer medium to the tubular reactor of the polyamide synthesis system to provide a used second flowable heat transfer medium, and allowing the used second flowable The heat medium is circulated back to the state of heat transfer by the heated first flowable heat transfer medium, wherein the second flowable heat transfer medium and the heated second flowable heat transfer medium are disposed in the second heating circuit The second heating circuit is configured to control the pressure of the second heat transfer loop to control the saturation temperature of the second flowable heat transfer medium, wherein controlling the saturation temperature controls the temperature of the tubular reactor, the second The flowable heat transfer medium and the used second flowable heat transfer medium are substantially liquid phase, the heated second flowable heat transfer medium is a substantially liquid phase, and the second flowable heat transfer medium is Passing the heat and passing the second flowable The heat transferred by the medium comprises 70-100% latent heat and 0-30% sensible heat, the latent heat comprising heat of vaporization; wherein the tubular reactor comprises a length of 75 to 125 meters, and the tubular reactor comprises 25 cm to 60 cm The inner diameter, the tubular reactor comprises a length/diameter (L/D) of from 100 to 500, and wherein the tubular reactor comprises from 10 to 25 discharge ports along its length.