Reactor and polyethylene polyamine synthesis system

Abstract

The invention relates to the technical field of chemical equipment, in particular to a reactor and a polyethylene polyamine synthesis system. The reactor comprises: a housing provided with a gas feed port, a plurality of liquid feed ports, a plurality of first discharge ports and a second discharge port; the plurality of reaction beds are arranged at intervals along the height direction of the shell; the multiple discharging pipelines are connected with the multiple reaction beds in a one-to-one correspondence mode, each discharging pipeline comprises a first branch pipe and a second branch pipe, the first branch pipes of the multiple discharging pipelines are connected with the multiple first discharging openings in a one-to-one correspondence mode, and the second branch pipes of the discharging pipelines connected with the upstream reaction beds are configured to provide raw materials for the downstream reaction beds; and the second branch pipe of the discharge pipeline connected with the most downstream reaction bed is connected with the second discharge port. The proportion of a liquid raw material to a gas raw material can be adjusted for different reaction beds, the ethylene glycol conversion rate and polyethylene polyamine product distribution are effectively regulated and controlled, and the process economy of polyethylene polyamine production by an ethylene glycol method is improved.

Description

Technical Field

[0001] The present application relates to the technical field of chemical equipment, and in particular to a reactor and a polyethylene polyamine synthesis system. Background Art

[0002] Polyethylene polyamine is a general term for organic amine fine chemical products, mainly including linear amine compounds such as ethylenediamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, and cyclic amine compounds such as piperazine, aminoethylpiperazine, and hydroxyethylpiperazine. Polyethylene polyamine is an important organic chemical raw material and is widely used in the fields of petroleum, medicine, pesticides, chemical fiber, textile, papermaking, surfactants, etc.

[0003] At present, polyethylene polyamines are mainly produced by the ethylene dichloride method, the ethanolamine method and the ethylene glycol method according to the raw material route. The ethylene dichloride method is gradually being eliminated due to the high energy consumption in the production process, serious equipment corrosion, high investment cost, and serious environmental pollution caused by "three wastes". The ethanolamine method has high raw material costs and needs to be built in areas with rich ethanolamine resources. The ethylene glycol method has the advantages of a wide source of raw materials and low raw material costs, but some ethylene glycol methods use a two-stage reaction process to ensure the conversion rate of ethylene glycol.

[0004] However, the products of the ethylene glycol method are mainly ethylenediamine, and the proportion of other products with tighter market demand is relatively small, which reduces the process economy of producing polyethylene polyamines by the ethylene glycol method. Summary of the invention

[0005] Based on this, the present application provides a reactor and a polyethylene polyamine synthesis system to solve the problem that the products of the ethylene glycol method for producing polyethylene polyamines in the related technology are mainly ethylenediamine, while the proportion of other products with tighter market demand is relatively small, which reduces the process economy of the ethylene glycol method for producing polyethylene polyamines.

[0006] In one aspect, the present application provides a reactor, comprising:

[0007] The shell has a containing cavity, the top of the shell is provided with a gas feed port, the side wall of the shell is provided with a plurality of liquid feed ports and a plurality of first discharge ports, and the bottom of the shell is provided with a second discharge port;

[0008] A plurality of reaction beds, the plurality of reaction beds are arranged at intervals along the height direction of the shell, the number of the reaction beds is the same as the number of the liquid feed ports, and the plurality of liquid feed ports are configured to provide liquid raw materials to the plurality of reaction beds in a one-to-one correspondence;

[0009] Multiple discharge pipelines are connected to the multiple reaction beds in a one-to-one manner, each discharge pipeline includes a first branch pipe and a second branch pipe, the first branch pipes of the multiple discharge pipelines are connected to the multiple first discharge ports in a one-to-one manner, the second branch pipe of the discharge pipeline connected to the upstream reaction bed is configured to provide raw materials to the downstream reaction bed, and the second branch pipe of the discharge pipeline connected to the most downstream reaction bed is connected to the second discharge port.

[0010] In a possible implementation, each reaction bed includes a plurality of reaction tubes, the plurality of reaction tubes of the reaction bed are located at the same height and arranged in parallel with each other, each reaction tube is connected to a discharge pipeline, and each reaction tube contains a catalyst;

[0011] The discharge pipeline also includes a main pipe and multiple third branches, the multiple third branches are respectively connected to one end of the main pipe, the first branch and the second branch are respectively connected to the other end of the main pipe, and the multiple third branches are connected to multiple reaction tubes one by one at one end away from the main pipe.

[0012] In a possible implementation, a gas-liquid distributor is disposed on the top of each reaction bed, and the gas-liquid distributor is configured to transport raw materials to a plurality of reaction tubes of the reaction bed.

[0013] In a possible implementation, the gas-liquid distributor includes a first bottom plate, a second bottom plate, and a plurality of downcomers located between the first bottom plate and the second bottom plate, and the first bottom plate and the second bottom plate are respectively fixed to the shell;

[0014] A plurality of first through holes are arranged on the first bottom plate, the plurality of first through holes are connected to the plurality of downcomers in a one-to-one correspondence, and the ends of the plurality of downcomers away from the first bottom plate are connected to the plurality of reaction tubes in a one-to-one correspondence.

[0015] In a possible implementation, the reactor further includes a plurality of liquid distribution pipes, the plurality of liquid distribution pipes are connected to the plurality of liquid feed ports in a one-to-one correspondence, and a plurality of spray holes are provided on the liquid distribution pipes.

[0016] In a possible implementation, the liquid distribution pipe includes a main path and multiple branches, one end of the main path is connected to the liquid feed port, and the multiple branches are respectively connected to the side walls of the main path, and the main path and each branch are respectively provided with multiple spray holes.

[0017] In a possible implementation, a pressure monitoring unit and a temperature monitoring unit are respectively installed at positions of the side walls of the shell corresponding to the reaction beds.

[0018] On the other hand, the present application also provides a polyethylene polyamine synthesis system, comprising a gas raw material heat exchange unit, a liquid raw material heat exchange unit, a deamination unit, a deweighting tower, a first distillation unit and the above-mentioned reactor, the discharge port of the gas raw material heat exchange unit is connected to the gas feed port of the reactor, the discharge port of the liquid raw material heat exchange unit is respectively connected to multiple liquid feed ports of the reactor, each first discharge port and second discharge port of the reactor is respectively connected to the feed port of the deamination unit, the first outlet of the deamination unit is connected to the feed port of the gas raw material heat exchange unit, the second outlet of the deamination unit is connected to the feed port of the deweighting tower, the first outlet of the deweighting tower is connected to the feed port of the first distillation unit, and the first outlet of the first distillation unit is connected to the feed port of the liquid raw material heat exchange unit.

[0019] In a possible implementation, the polyethylene polyamine synthesis system further includes a dehydration unit, the second outlet of the deamination unit is connected to the feed inlet of the dehydration unit, and the second outlet of the dehydration unit is connected to the feed inlet of the deweighting tower.

[0020] In a possible implementation, the polyethylene polyamine synthesis system also includes a first storage tank, a second storage tank, a third storage tank and a second distillation unit, the first outlet of the dehydration unit is connected to the first storage tank, the second outlet of the first distillation unit is connected to the second storage tank, the second outlet of the deweighting tower is connected to the feed inlet of the second distillation unit, and the outlet of the second distillation unit is connected to the third storage tank.

[0021] The reactor and polyethylene polyamine synthesis system provided by the present application are provided with a plurality of liquid feed ports, a plurality of first discharge ports and a second discharge port on the shell of the reactor, and a plurality of reaction beds are provided inside the shell. The plurality of liquid feed ports can provide liquid raw materials to the plurality of reaction beds in a one-to-one correspondence, and the flow direction of the products after the reaction of the reaction beds can be controlled by adjusting the main material pipeline. In this way, the ratio of liquid raw materials to gaseous raw materials can be adjusted for different reaction beds, and the conversion rate of ethylene glycol and the distribution of polyethylene polyamine products can be effectively regulated. In addition, the reactor provided by the present application integrates many reactor functions of ethylene glycol synthesis of different types of polyethylene polyamine products into one reactor, which promotes the improvement of the synthesis efficiency of polyethylene polyamines, optimizes costs, and increases benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the following is a brief introduction to the drawings required for use in the embodiments or the description of the prior art.

[0023] Figure 1 A schematic diagram of the structure of a reactor provided in an embodiment of the present application;

[0024] Figure 2 This is a schematic diagram of the structure of the polyethylene polyamine synthesis system provided in the embodiments of the present application.

[0025] Description of reference numerals:

[0026] 100-reactor;

[0027] 110-shell; 111-accommodating chamber; 112-gas feed port; 113-liquid feed port; 114-first discharge port; 115-second discharge port;

[0028] 120-reaction bed; 121-reaction tube; 122-catalyst;

[0029] 130-discharging pipeline; 131-main pipe; 132-first branch pipe; 133-second branch pipe; 134-third branch pipe;

[0030] 140-gas-liquid distributor; 141-first bottom plate; 142-second bottom plate; 143-downcomer;

[0031] 150-liquid distribution pipe; 151-main line; 152-branch line;

[0032] 161-pressure monitoring unit; 162-temperature monitoring unit;

[0033] 200-gas raw material heat exchange unit; 300-liquid raw material heat exchange unit; 400-deammoniation unit; 500-deweighting tower; 600-first distillation unit; 700-dehydration unit; 800-second distillation unit; 910-first storage tank; 920-second storage tank; 930-third storage tank.

[0034] The above drawings have shown clear embodiments of the present application, which will be described in more detail later. These drawings and text descriptions are not intended to limit the scope of the present application in any way, but to illustrate the concept of the present application to those skilled in the art by referring to specific embodiments. DETAILED DESCRIPTION

[0035] In order to make the purpose, technical scheme and advantages of the present application clearer, the technical scheme in the embodiment of the present application will be described in more detail below in conjunction with the drawings in the preferred embodiments of the present application. In the drawings, the same or similar reference numerals throughout represent the same or similar parts or parts with the same or similar functions. The described embodiments are part of the embodiments of the present application, not all of the embodiments. The embodiments described below with reference to the drawings are exemplary and are intended to be used to explain the present application, and should not be construed as limitations on the present application. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present application. The embodiments of the present application are described in detail below in conjunction with the drawings.

[0036] In the description of this application, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, or it can be an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0037] In the description of the present application, it should be understood that the terms "upper", "lower", "front", "back", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating orientations or positional relationships, are orientations or positional relationships based on the drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present application.

[0038] The terms "first", "second" and "third" (if any) in the specification and claims of this application and the above drawings are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence.

[0039] In addition, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, for example, a process, method, system, product, or display comprising a series of steps or elements is not necessarily limited to those steps or elements explicitly listed, but may include other steps or elements not explicitly listed or inherent to such process, method, product, or display.

[0040] In the prior art, polyethylene polyamines are mainly produced by the ethylene dichloride method, the ethanolamine method and the ethylene glycol method according to the raw material route. The ethylene glycol method has the advantages of a wide source of raw materials and low raw material costs. Some ethylene glycol methods use a two-stage reaction process to ensure the conversion rate of ethylene glycol. The production of polyethylene polyamines by the ethylene glycol method requires multiple reactors in series to increase the conversion rate of ethylene glycol. However, the proportion of ethylenediamine in the polyethylene polyamine product is relatively high, and the proportion of other products with tighter market demand is relatively small, which reduces the process economy of producing polyethylene polyamines by the ethylene glycol method.

[0041] After repeated thinking and verification, the inventors found that if multiple reaction beds are set inside the shell of the reactor to ensure the conversion rate of ethylene glycol, multiple liquid feed ports are set on the shell, and the multiple liquid feed ports can provide liquid raw materials to the multiple reaction beds respectively. Multiple reaction beds are respectively connected to multiple discharge pipelines, and the product after the reaction of the previous reaction bed can flow to the next reaction bed or discharge the reactor. In this way, the ratio of liquid raw materials to gas raw materials can be adjusted for different reaction beds, and the flow direction of the product after the reaction of the reaction bed can be controlled, so as to effectively regulate the conversion rate of ethylene glycol and the distribution of polyethylene polyamine products, and improve the process economy of producing polyethylene polyamines by the ethylene glycol method.

[0042] In view of this, the inventors have designed a reactor and a polyethylene polyamine synthesis system, wherein multiple reaction beds are arranged in the shell of the reactor, a gas feed port and multiple liquid feed ports are arranged on the shell, and the multiple liquid feed ports can provide liquid raw materials to the multiple reaction beds in a one-to-one correspondence. The ratio between the gas raw material and the liquid raw material can be adjusted for different reaction beds, and the ethylene glycol conversion rate and the polyethylene polyamine product distribution can be effectively regulated. At the same time, the reactor is provided with multiple discharge pipelines, and the multiple discharge pipelines are respectively connected to the multiple reaction beds. By controlling the state of the discharge pipeline, the flow direction of the product after the reaction of the reaction bed can be controlled, and the ethylene glycol conversion rate and the polyethylene polyamine product distribution can be further regulated.

[0043] The technical scheme of the reactor and the polyethylene polyamine synthesis system provided in the embodiments of the present application is described in detail below in conjunction with the accompanying drawings.

[0044] Reference Figure 1 As shown, the reactor 100 provided in the embodiment of the present application can be used to produce polyethylene polyamines, and the reactor 100 includes a shell 110, a plurality of reaction beds 120, and a plurality of discharge pipes 130. The shell 110 has a accommodating chamber 111, a gas feed port 112 is provided at the top of the shell 110, a plurality of liquid feed ports 113 and a plurality of first discharge ports 114 are provided on the side wall of the shell 110, and a second discharge port 115 is provided at the bottom of the shell 110. The plurality of reaction beds 120 are arranged at intervals along the height direction of the shell 110, and the number of the reaction beds 120 is the same as the number of the liquid feed ports 113, and the plurality of liquid feed ports 113 are configured to provide liquid raw materials to the plurality of reaction beds 120 in a one-to-one correspondence. The plurality of discharge pipelines 130 are connected to the plurality of reaction beds 120 in a one-to-one correspondence, and each discharge pipeline 130 includes a first branch pipe 132 and a second branch pipe 133. The first branch pipes 132 of the plurality of discharge pipelines 130 are connected to the plurality of first discharge ports 114 in a one-to-one correspondence. The second branch pipe 133 of the discharge pipeline 130 connected to the upstream reaction bed 120 is configured to provide raw materials to the downstream reaction bed 120, and the second branch pipe 133 of the discharge pipeline 130 connected to the most downstream reaction bed 120 is connected to the second discharge port 115.

[0045] Schematically, the gas feed port 112 of the shell 110 can be used to introduce ammonia and hydrogen, and the liquid feed port 113 of the shell 110 can be used to introduce ethylene glycol. Ammonia, hydrogen and ethylene glycol react in the reaction bed 120 to generate polyethylene polyamine. Among them, the number of reaction beds 120, the number of liquid feed ports 113 and the number of discharge pipelines 130 are the same and at least two, which is not limited here. This embodiment does not limit the size of the interval between two adjacent reaction beds 120, and those skilled in the art can set it as needed.

[0046] It is worth mentioning that the staff can control the amount of ethylene glycol introduced into the corresponding liquid feed port 113 according to different reaction beds 120, thereby controlling the ratio of gas raw materials to liquid raw materials in the reaction bed 120, and can also adjust the hydrogen partial pressure by adjusting the ratio of hydrogen and ammonia in the gas introduced into the gas feed port 112. The above settings can not only efficiently promote the reaction, but also effectively control the product composition distribution.

[0047] In one possible implementation, the first branch pipe 132 and the second branch pipe 133 of each discharge pipeline 130 are respectively provided with a switch valve. When the switch valve on the first branch pipe 132 is opened and the switch valve on the second branch pipe 133 is closed, the product of the reaction bed 120 connected to the discharge pipeline 130 can flow out from the corresponding first discharge port 114; when the switch valve on the first branch pipe 132 is closed and the switch valve on the second branch pipe 133 is opened, the product of the upstream reaction bed 120 can flow to the top of the downstream reaction bed 120 and continue to participate in the reaction in the downstream reaction bed 120.

[0048] The reactor 100 provided in this embodiment is provided with a plurality of liquid feed ports 113, a plurality of first discharge ports 114 and a second discharge port 115 on the shell 110, and a plurality of reaction beds 120 are provided inside the shell 110. The plurality of liquid feed ports 113 can provide liquid raw materials to the plurality of reaction beds 120 one by one, and the flow direction of the products after the reaction of the reaction beds 120 can be controlled by adjusting the main material pipeline. The reactor 100 provided in this embodiment integrates the functions of many reactors 100 for synthesizing different types of polyethylene polyamine products from ethylene glycol into one reactor 100, promotes the improvement of polyethylene polyamine synthesis efficiency, optimizes costs, and increases benefits. When producing polyethylene polyamine, it is not necessary to set up a plurality of reaction devices in series. The reactor 100 is flexible in operation. When working, it can adjust the ratio of liquid raw materials to gas raw materials for different reaction beds 120, and effectively regulate the conversion rate of ethylene glycol and the distribution of polyethylene polyamine products.

[0049] In one embodiment, Figure 1As shown, each reaction bed 120 includes a plurality of reaction tubes 121. The plurality of reaction tubes 121 of the reaction bed 120 are located at the same height and arranged in parallel with each other, and each reaction tube 121 is respectively connected to a discharge pipeline 130, and each reaction tube 121 contains a catalyst 122. The discharge pipeline 130 includes a main pipe 131 and a plurality of third branch pipes 134, the plurality of third branch pipes 134 are respectively connected to one end of the main pipe 131, the first branch pipe 132 and the second branch pipe 133 are respectively connected to the other end of the main pipe 131, and the plurality of third branch pipes 134 are connected to the plurality of reaction tubes 121 in a one-to-one correspondence at one end away from the main pipe 131.

[0050] Schematically, at the same height position of the shell 110, a plurality of reaction tubes 121 are arranged along the radial direction of the shell 110. Specifically, the plurality of reaction tubes 121 of the reaction bed 120 are arranged at equal intervals in the annular direction along the center of the shell 110, that is, the plurality of reaction tubes 121 of the reaction bed 120 are arranged in a plurality of concentric rings, and the plurality of reaction tubes 121 in each ring are arranged at equal intervals.

[0051] Figure 1 As shown, the plurality of reaction tubes 121 are connected to one end of the main tube 131 through the plurality of third branch tubes 134 , and the first branch tube 132 and the second branch tube 133 may be connected to the other end of the main tube 131 .

[0052] It should be noted that the catalysts 122 in the reaction tubes 121 of different reaction beds 120 may be the same or different, and those skilled in the art may set the catalysts 122 in the specific reaction tubes 121 as needed, which is not limited here. The sizes of the reaction tubes 121 of different reaction beds 120 may be the same or different, which is not limited here.

[0053] The above arrangement enables the reaction bed 120 to accommodate enough catalysts 122. The liquid raw materials react with the gas raw materials in the reaction tubes 121. The heat generated during the reaction can be discharged from the gaps between the reaction tubes 121, ensuring that the reaction bed 120 has sufficient reaction capacity.

[0054] In a specific embodiment, a gas-liquid distributor 140 is disposed on the top of each reaction bed 120 , and the gas-liquid distributor 140 is configured to transport raw materials to the multiple reaction tubes 121 of the reaction bed 120 .

[0055] The liquid feed port 113 is located above the gas-liquid distributor 140 on the corresponding reaction bed 120, and the ethylene glycol input from the liquid feed port 113 and the hydrogen and ammonia input from the gas feed port 112 are mixed above the reaction bed 120. Optionally, the gas-liquid distributor 140 is provided with a plurality of passages, and the number of the passages may be the same as the number of the reaction tubes 121 below the gas-liquid distributor 140, and the mixture of ethylene glycol, hydrogen and ammonia may be input into the reaction tubes 121 of the reaction bed 120 through the plurality of passages of the gas-liquid distributor 140.

[0056] By arranging the gas-liquid distributor 140 above the reaction bed 120 , it is prevented that the raw material mixture enters the gap between the reaction tubes 121 and reduces the conversion rate of ethylene glycol.

[0057] Specifically, if Figure 1 As shown, the gas-liquid distributor 140 includes a first bottom plate 141 , a second bottom plate 142 and a plurality of downcomers 143 located between the first bottom plate 141 and the second bottom plate 142 . The first bottom plate 141 and the second bottom plate 142 are fixed to the shell 110 , respectively.

[0058] The first bottom plate 141 is provided with a plurality of first through holes, which are connected to the plurality of downcomers 143 in a one-to-one correspondence, and one end of the plurality of downcomers 143 away from the first bottom plate 141 is connected to the plurality of reaction tubes 121 in a one-to-one correspondence.

[0059] Schematically, the number of downcomers 143 is the same as the number of reaction tubes 121 , and the multiple downcomers 143 are coaxially arranged with the multiple reaction tubes 121 . Figure 1 As shown, the top end of each downcomer 143 is fixed to the first bottom plate 141, and the bottom end is fixed to the second bottom plate 142. The first bottom plate 141 and the second bottom plate 142 can be fixed to the housing 110 by fastening with fasteners, bonding or welding, etc., which is not limited here.

[0060] Optionally, a plurality of first through holes are provided on the first bottom plate 141, a plurality of second through holes are provided on the second bottom plate 142, the top end of the downcomer 143 is communicated with the first through holes, and the bottom end of the downcomer 143 is communicated with the second through holes. It can be understood that the downcomer 143 serves as a passage of the gas-liquid distributor 140, and the mixture of ethylene glycol, hydrogen and ammonia can be input into the reaction tubes 121 of the reaction bed 120 through the downcomer 143, the first through holes on the first bottom plate 141 and the second through holes on the second bottom plate 142, so as to prevent the raw material mixture from entering the gaps between the reaction tubes 121.

[0061] Figure 1 As shown, the reactor 100 further includes a plurality of liquid distribution pipes 150 , and the plurality of liquid distribution pipes 150 are connected to the plurality of liquid feed ports 113 in a one-to-one correspondence, and a plurality of spray holes are disposed on the liquid distribution pipes 150 .

[0062] Schematically, one end of the liquid distribution pipe 150 is connected to the liquid feed port 113, and the ethylene glycol liquid enters the liquid distribution pipe 150 through the liquid feed port 113. The liquid in the liquid distribution pipe 150 can be sprayed from the spray hole in the liquid distribution pipe 150 to the inside of the accommodating chamber 111 to achieve full mixing of the liquid raw material and the gas raw material to ensure the conversion rate of ethylene glycol. This embodiment does not limit the number of spray holes and the specific positions of the spray holes on the liquid distribution pipe 150, and those skilled in the art can set them as needed.

[0063] Specifically, the liquid distribution pipe 150 includes a main passage 151 and a plurality of branches 152. One end of the main passage 151 is connected to the liquid feed port 113, and the plurality of branches 152 are respectively connected to the side walls of the main passage 151. The main passage 151 and each branch 152 are respectively provided with a plurality of spray holes.

[0064] Pipes may be used as the main path 151 and the branch paths 152 of the liquid distribution pipe 150, the extension direction of each branch path 152 may be perpendicular to the extension direction of the main path 151, and one end of the main path 151 away from the liquid feed port 113 may extend to a side of the housing 110 away from the liquid feed port 113. The ethylene glycol entering through the liquid feed port 113 may flow from the main path 151 to each branch path 152.

[0065] Through the above arrangement, the ethylene glycol in the main path 151 of the liquid distribution pipe 150 can be sprayed into the interior of the containing chamber 111 through the spray holes on the main path 151, and the ethylene glycol in each branch path 152 can be sprayed into the interior of the containing chamber 111 through the spray holes on the corresponding branch paths 152, thereby ensuring the spray range of the ethylene glycol liquid in the containing chamber 111, so that the liquid raw material can be further fully mixed with the gas raw material.

[0066] like Figure 1 As shown, a pressure monitoring unit 161 and a temperature monitoring unit 162 are respectively installed on the side wall of the shell 110 at positions corresponding to each reaction bed 120 .

[0067] The detection end of the pressure monitoring unit 161 and the detection end of the temperature monitoring unit 162 are both directed toward the reaction tube 121 of the corresponding reaction bed 120. Schematically, a pressure sensor can be used as the pressure monitoring unit 161, and a temperature sensor can be used as the temperature monitoring unit 162. It can be understood that the pressure monitoring unit 161 can detect the pressure inside the shell 110 at the position of the reaction bed 120, and the temperature monitoring unit 162 can detect the temperature inside the shell 110 at the position of the reaction bed 120.

[0068] In this structure, the staff can obtain the pressure and temperature at different positions of the reaction bed 120 through the pressure monitoring unit 161 and the temperature monitoring unit 162, so as to control the pressure and temperature at the position of the reaction bed 120, on the one hand, ensuring that the environment at the position of the reaction bed 120 can make the reaction proceed smoothly, and on the other hand, the energy consumption of the reactor 100 can be controlled by the pressure and temperature at the position of the reaction bed 120. In addition, by regulating the temperature and pressure of the reaction, not only the reaction is efficiently promoted, but also the product composition distribution can be controlled.

[0069] The present application also provides a polyethylene polyamine synthesis system, such as Figure 2 As shown, it includes a gas raw material heat exchange unit 200, a liquid raw material heat exchange unit 300, a deamination unit 400, a deweighting tower 500, a first distillation unit 600 and the above-mentioned reactor 100. The discharge port of the gas raw material heat exchange unit 200 is connected to the gas feed port 112 of the reactor 100, and the discharge port of the liquid raw material heat exchange unit 300 is respectively connected to multiple liquid feed ports 113 of the reactor 100. Each first discharge port 114 and second discharge port 115 of the reactor 100 is respectively connected to the feed port of the deamination unit 400, the first outlet of the deamination unit 400 is connected to the feed port of the gas raw material heat exchange unit 200, and the second outlet of the deamination unit 400 is connected to the feed port of the deweighting tower 500. The first outlet of the deweighting tower 500 is connected to the feed port of the first distillation unit 600, and the first outlet of the first distillation unit 600 is connected to the feed port of the liquid raw material heat exchange unit 300.

[0070] Among them, heat exchangers can be used as the gas raw material heat exchange unit 200 and the liquid raw material heat exchange unit 300, respectively. The gas raw material heat exchange unit 200 can preheat the gas raw materials, i.e., hydrogen and ammonia, and the liquid raw material heat exchange unit 300 can preheat the liquid raw material, i.e., ethylene glycol. Optionally, a gas-liquid separator can be used as the deamination unit 400, and the gas in the discharged material of the reactor 100 can be separated by the deamination unit 400, and the separated gas flows out from the first outlet of the deamination unit 400 and flows back to the gas raw material heat exchange unit 200 for reuse.

[0071] The liquid separated by the deamination unit 400 flows out from the second outlet and flows into the deweighting tower 500. The deweighting tower 500 can separate the light component material and the heavy component material entering the liquid, and the light component material flows out from the first outlet of the deweighting tower 500 and flows into the first distillation unit 600. Among them, the molecular weight of the light component material is less than the molecular weight of the heavy component material.

[0072] The first distillation unit 600 can separate the inflowing light component material into unreacted raw materials, namely ethylene glycol and light component products. The unreacted raw materials flow out from the first outlet of the first distillation unit 600 and enter the liquid raw material heat exchange unit 300 for reuse.

[0073] With this structure, the unreacted gas raw material flowing out of the reactor 100 can flow back to the gas raw material heat exchange unit 200, and the unreacted liquid raw material flowing out of the reactor 100 can flow back to the liquid raw material heat exchange unit 300, thereby efficiently recycling the ethylene glycol and ammonia raw materials and reducing raw material loss.

[0074] In one embodiment, Figure 2 As shown, the polyethylene polyamine synthesis system further includes a dehydration unit 700. The second outlet of the deamination unit 400 is connected to the feed inlet of the dehydration unit 700, and the second outlet of the dehydration unit 700 is connected to the feed inlet of the deweight removal column 500.

[0075] A distillation tower can be used as the dehydration unit 700, and the dehydration unit 700 can separate the water flowing into the liquid. Specifically, the liquid flowing out from the second outlet of the deamination unit 400 includes a mixture and water. After the mixture and water flow into the dehydration unit 700, the dehydration unit 700 separates the water therein, and the separated dehydrated component flows into the deweighting tower 500 from the second outlet of the dehydration unit 700.

[0076] In this structure, the liquid flowing out of the deamination unit 400 first enters the dehydration unit 700 for dehydration, and the dehydrated mixture then enters the subsequent device for separation. The polyethylene polyamine synthesis system does not need to set up multiple dehydration mechanisms, which effectively reduces the complexity of the subsequent separation process and equipment, shortens the process flow and reduces energy consumption.

[0077] Figure 2 It is shown that the polyethylene polyamine synthesis system also includes a first storage tank 910, a second storage tank 920, a third storage tank 930 and a second distillation unit 800, the first outlet of the dehydration unit 700 is connected to the first storage tank 910, the second outlet of the first distillation unit 600 is connected to the second storage tank 920, the second outlet of the deweighting tower 500 is connected to the feed port of the second distillation unit 800, and the discharge port of the second distillation unit 800 is connected to the third storage tank 930.

[0078] The first storage tank 910 can be used as a wastewater storage tank, and the water separated by the dehydration unit 700 can be stored in the first storage tank 910, so as to facilitate the subsequent centralized treatment of the separated water. The second storage tank 920 can be used as a light component product storage tank, and the light component product separated by the first distillation unit 600 can be stored in the second storage tank 920.

[0079] Illustratively, the heavy component material separated by the deweighting tower 500 can flow into the second distillation unit 800 from the second outlet, and the discharge port of the second distillation unit 800 can output the heavy component product. The third storage tank 930 can be used as a heavy component product storage tank, and the heavy component product output from the second distillation unit 800 can be stored in the third storage tank 930.

[0080] In this structure, the heavy component material separated by the deweighting tower 500 can be used to obtain the heavy component product through the second distillation unit 800, the water separated by the dehydration unit 700 is stored in the first storage tank 910, the light component product is stored in the second storage tank 920, and the heavy component product is stored in the third storage tank 930, thereby realizing the separation and storage of different component products.

[0081] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit it. Although the present application has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A reactor (100), characterized in that: include: A shell (110) having a containing cavity (111), a gas feed port (112) being arranged at the top end of the shell (110), a plurality of liquid feed ports (113) and a plurality of first discharge ports (114) being arranged at the side wall of the shell (110), and a second discharge port (115) being arranged at the bottom end of the shell (110); a plurality of reaction beds (120), the plurality of reaction beds (120) being arranged at intervals along the height direction of the shell (110), the number of the reaction beds (120) being the same as the number of the liquid feed ports (113), and the plurality of liquid feed ports (113) being configured to provide liquid raw materials to the plurality of reaction beds (120) in a one-to-one correspondence; A plurality of discharge pipelines (130), wherein the plurality of discharge pipelines (130) are connected to the plurality of reaction beds (120) in a one-to-one correspondence, each of the discharge pipelines (130) comprises a first branch pipe (132) and a second branch pipe (133), the first branch pipes (132) of the plurality of discharge pipelines (130) are connected to the plurality of first discharge ports (114) in a one-to-one correspondence, the second branch pipe (133) of the discharge pipeline (130) connected to the upstream reaction bed (120) is configured to provide raw materials to the downstream reaction bed (120), and the second branch pipe (133) of the discharge pipeline (130) connected to the most downstream reaction bed (120) is connected to the second discharge port (115).

2. The reactor (100) according to claim 1, characterized in that Each of the reaction beds (120) comprises a plurality of reaction tubes (121), the plurality of reaction tubes (121) of the reaction bed (120) are located at the same height and arranged in parallel with each other, each of the reaction tubes (121) is respectively connected to the discharge pipeline (130), and each of the reaction tubes (121) contains a catalyst (122); The discharge pipeline (130) further comprises a main pipe (131) and a plurality of third branch pipes (134); the plurality of third branch pipes (134) are respectively connected to one end of the main pipe (131); the first branch pipe (132) and the second branch pipe (133) are respectively connected to the other end of the main pipe (131); and one end of the plurality of third branch pipes (134) away from the main pipe (131) is connected to the plurality of reaction tubes (121) in a one-to-one correspondence.

3. The reactor (100) according to claim 2, characterized in that A gas-liquid distributor (140) is disposed on the top of each reaction bed (120), and the gas-liquid distributor (140) is configured to transport raw materials to the multiple reaction tubes (121) of the reaction bed (120).

4. The reactor (100) according to claim 3, characterized in that The gas-liquid distributor (140) comprises a first bottom plate (141), a second bottom plate (142), and a plurality of downcomers (143) located between the first bottom plate (141) and the second bottom plate (142), wherein the first bottom plate (141) and the second bottom plate (142) are respectively fixed to the shell (110); The first bottom plate (141) is provided with a plurality of first through holes, the plurality of first through holes are connected to the plurality of downcomers (143) in a one-to-one correspondence, and one end of the plurality of downcomers (143) away from the first bottom plate (141) is connected to the plurality of reaction tubes (121) in a one-to-one correspondence.

5. The reactor (100) according to claim 1, characterized in that The reactor (100) further comprises a plurality of liquid distribution pipes (150), wherein the plurality of liquid distribution pipes (150) are connected to the plurality of liquid feed ports (113) in a one-to-one correspondence, and the liquid distribution pipes (150) are provided with a plurality of spray holes.

6. The reactor (100) according to claim 5, characterized in that The liquid distribution pipe (150) includes a main path (151) and a plurality of branch paths (152), one end of the main path (151) is connected to the liquid feed port (113), and the plurality of branch paths (152) are respectively connected to the side walls of the main path (151), and the main path (151) and each of the branch paths (152) are respectively provided with a plurality of spray holes.

7. The reactor (100) according to any one of claims 1 to 6, characterized in that: A pressure monitoring unit (161) and a temperature monitoring unit (162) are respectively installed on the side wall of the shell (110) at positions corresponding to the reaction beds (120).

8. A polyethylene polyamine synthesis system, characterized in that: The invention comprises a gas raw material heat exchange unit (200), a liquid raw material heat exchange unit (300), a deamination unit (400), a deweighting tower (500), a first distillation unit (600) and a reactor (100) according to any one of claims 1 to 7, wherein the outlet of the gas raw material heat exchange unit (200) is connected to the gas feed port (112) of the reactor (100), the outlet of the liquid raw material heat exchange unit (300) is respectively connected to the multiple liquid feed ports (113) of the reactor (100), and the first outlet ports of the reactor (100) are connected to the gas feed port (112) of the reactor (100). The feed port (114) and the second discharge port (115) are respectively connected to the feed port of the deamination unit (400); the first outlet of the deamination unit (400) is connected to the feed port of the gas raw material heat exchange unit (200); the second outlet of the deamination unit (400) is connected to the feed port of the deweighting tower (500); the first outlet of the deweighting tower (500) is connected to the feed port of the first distillation unit (600); and the first outlet (114) of the first distillation unit (600) is connected to the feed port of the liquid raw material heat exchange unit (300).

9. The polyethylene polyamine synthesis system according to claim 8, characterized in that: The polyethylene polyamine synthesis system further comprises a dehydration unit (700), the second outlet of the deamination unit (400) is connected to the feed inlet of the dehydration unit (700), and the second outlet of the dehydration unit (700) is connected to the feed inlet of the deweight removal tower (500).

10. The polyethylene polyamine synthesis system according to claim 9, characterized in that: The polyethylene polyamine synthesis system further comprises a first storage tank (910), a second storage tank (920), a third storage tank (930) and a second distillation unit (800), wherein a first outlet of the dehydration unit (700) is connected to the first storage tank (910), a second outlet of the first distillation unit (600) is connected to the second storage tank (920), a second outlet of the deweighting tower (500) is connected to a feed port of the second distillation unit (800), and an outlet of the second distillation unit (800) is connected to the third storage tank (930).

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