CN214400309U - System for synthesizing acetic acid by methanol low-pressure carbonyl for recycling reaction heat - Google Patents
System for synthesizing acetic acid by methanol low-pressure carbonyl for recycling reaction heat Download PDFInfo
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- CN214400309U CN214400309U CN202022903058.0U CN202022903058U CN214400309U CN 214400309 U CN214400309 U CN 214400309U CN 202022903058 U CN202022903058 U CN 202022903058U CN 214400309 U CN214400309 U CN 214400309U
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Abstract
The utility model discloses a system for synthesizing acetic acid by methanol low-pressure carbonyl for reaction heat recycling, in the system, a power circulating pump and a heat recovery heat exchanger are sequentially connected between a reaction liquid outlet and a reaction liquid inlet, a tube side and a shell side of the heat recovery heat exchanger are respectively communicated with the reaction liquid inlet and a boiler water outlet, and a product outlet of a reaction kettle is connected with an evaporator; the gas phase outlet of the evaporator is sequentially connected with a light component removal tower, a dehydration tower and a finished product tower; the gas phase outlet of the light component removal tower is connected with a dealkylation tower; the bottom of the dehydration tower is sequentially connected in series with a dehydration tower preheating reboiler and a tower bottom reboiler of the dehydration tower; the bottom of the finished product tower is sequentially connected in series with a finished product tower preheating reboiler and a finished product tower bottom reboiler; the shell pass outlet of the heat recovery heat exchanger is connected with a lightness-removing tower reboiler, a dehydration tower preheating reboiler and a finished product tower preheating reboiler, and a pipeline of the shell pass outlet of the heat recovery heat exchanger is provided with a back pressure valve; the tower bottom reboiler of the dehydration tower and the tower bottom reboiler of the finished product tower are connected with a boiler steam source. The system can reduce energy consumption.
Description
Technical Field
The utility model relates to a system for synthesizing acetic acid by methanol low-pressure carbonyl for recycling reaction heat.
Background
The statements herein merely provide background information related to the present disclosure and may not necessarily constitute prior art.
Acetic acid, a systematic name for acetic acid, is a colorless liquid organic compound that is a chemical reagent for producing the compound. The largest single use of acetic acid is in the production of vinyl acetate monomer, followed by the production of acetic anhydride and esters. The vinegar contains relatively small amount of acetic acid. The preparation method of the acetic acid mainly comprises methanol carbonylation, acetaldehyde oxidation, ethylene oxidation, oxidative fermentation, anaerobic fermentation and the like. Currently, most acetic acid is prepared by a methanol carbonylation method, the methanol carbonylation method is divided into a high pressure method and a low pressure method, and the high pressure method has high energy consumption (the temperature is about 250 ℃) and high requirements on reaction equipment (the pressure is about 64 MPa) compared with the low pressure method, so the methanol low pressure carbonylation method for synthesizing the acetic acid becomes the most common acetic acid synthesis method.
The method for synthesizing acetic acid by methanol low-pressure carbonylation takes a rhodium-based compound as a catalyst, methyl iodide as a cocatalyst, and methanol and carbon monoxide are subjected to carbonylation reaction at the temperature of 150-200 ℃ and under the pressure of 2.7-3.0 MPa to generate acetic acid, wherein the process is an exothermic reaction. The inventor researches and discovers that a part of a large amount of reaction heat released in the reaction process of synthesizing acetic acid is removed in a mother liquor flash evaporation circulation mode, and the other part of the reaction heat is removed through a circulating water heat exchanger, so that a large amount of reaction heat is wasted.
SUMMERY OF THE UTILITY MODEL
In order to solve the deficiency of the prior art, the utility model aims at providing a system of methyl alcohol low pressure oxo acetic acid of reaction heat recycle can use methyl alcohol low pressure oxo acetic acid technology with reaction heat in the synthetic acetic acid reaction process, reduces the waste of reaction heat, reduces the demand of methyl alcohol low pressure oxo acetic acid technology to high-grade steam more than 1MPa simultaneously to reduce the energy consumption.
In order to realize the purpose, the technical scheme of the utility model is that:
a system for synthesizing acetic acid by methanol low-pressure carbonyl with reaction heat recycling comprises a reaction kettle, an evaporator, a light component removal tower, a dehydration tower and a finished product tower;
the reaction kettle is provided with a reaction liquid outlet, a reaction liquid inlet and a product outlet, a power circulating pump and a heat recovery heat exchanger are sequentially connected between the reaction liquid outlet and the reaction liquid inlet, the heat recovery heat exchanger is a shell-and-tube heat exchanger, the reaction liquid inlet is communicated with the tube side of the heat recovery heat exchanger, the shell side of the heat recovery heat exchanger is communicated with a boiler water outlet, and the product outlet of the reaction kettle is connected with an evaporator;
a gas phase outlet of the evaporator is connected with a light component removal tower, a gas phase outlet is formed in the top of the light component removal tower, a product outlet is formed in the middle of the light component removal tower, the gas phase outlet of the light component removal tower is connected with a dealkylation tower, and the product outlet of the light component removal tower is connected with a dehydration tower;
the bottom of the dehydration tower is sequentially connected in series with a dehydration tower preheating reboiler and a tower bottom reboiler of the dehydration tower, the bottom of the dehydration tower is provided with a product outlet, and the product outlet of the dehydration tower is connected with a finished product tower;
the bottom of the finished product tower is sequentially connected in series with a finished product tower preheating reboiler and a finished product tower bottom reboiler;
the shell pass outlet of the heat recovery heat exchanger is connected with a lightness-removing tower reboiler, a dehydration tower preheating reboiler and a finished product tower preheating reboiler, and a pipeline of the shell pass outlet of the heat recovery heat exchanger is provided with a back pressure valve;
the tower bottom reboiler of the dehydration tower and the tower bottom reboiler of the finished product tower are connected with a boiler steam source.
The utility model discloses through the research discovery, rectifying column (lightness-removing column, dehydration tower, finished product tower etc.) in the synthetic acetic acid technology of methyl alcohol low pressure carbonyl is all inequality to the requirement of temperature, the recovery heat in the synthetic acetic acid reaction process is difficult to satisfy the temperature requirement of these rectifying column simultaneously, discover through further research, when retrieving thermal steam control in the synthetic acetic acid reaction process at 0.6 ~ 0.8MPa (G), can satisfy lightness-removing column, dealkylation tower, the temperature demand of regenerator column, but still can't satisfy the temperature demand of part high temperature rectifying column (like dehydration tower, finished product tower etc.). Therefore the utility model discloses two reboilers are established ties at the bottom of this part high temperature rectifying column, and aim at adopts the steam of retrieving the heat to preheat, then adopts 1.2 ~ 1.4 MPa's steam to reheat, consumption that can greatly reduced 1.2 ~ 1.4 MPa's steam. In order to make the synthetic acetic acid reaction in-process retrieve thermal steam control at 0.6 ~ 0.8MPa (G), the utility model discloses a boiler water retrieves the heat in the reaction liquid in to reation kettle, boiler water itself has certain heat, the shell side that adopts the heat recovery heat exchanger again is boiler water, the tube side is the reaction liquid in the reation kettle, increase the endothermic effect of boiler water, adopt power circulating pump to pressurize the reaction liquid in the reation kettle, increase the back pressure valve simultaneously, adjust steam pressure, the realization utilizes the reaction heat in the synthetic acetic acid reaction to produce the saturated steam of 0.6 ~ 0.8MPa (G), thereby utilize the reaction heat in the synthetic acetic acid reaction to provide the heat to all rectifying columns in the synthetic acetic acid technology of methyl alcohol low pressure carbonyl, in order to reduce the synthetic acetic acid technology of methyl alcohol low pressure carbonyl to the consumption of former steam of 1.2 ~ 1.4 MPa.
Further, a gas phase outlet of the light component removal tower is connected with an inlet of a condenser at the top of the light component removal tower, an outlet of the condenser at the top of the light component removal tower is connected with a dealkylation tower, and a shell pass outlet of the heat recovery heat exchanger is connected with a reboiler at the bottom of the dealkylation tower. The gas-phase product of the light component removal tower can be reprocessed, and the reaction heat is further utilized, so that the energy consumption is reduced.
Furthermore, an outlet of a condenser at the top of the light component removal tower is connected with a delayer, and an outlet at the bottom of the delayer is connected with a dealkylation tower.
Furthermore, the outlet at the top of the delayer is connected with a low-pressure absorption tower, the outlet of the low-pressure absorption tower is connected with a regeneration tower, and the shell-side outlet of the heat recovery heat exchanger is connected with a reboiler at the bottom of the regeneration tower.
Furthermore, the middle outlet of the delayer is connected with the upper inlet of the light component removal tower.
Further, a gas phase outlet of the reaction kettle is connected with an inlet of a high-pressure absorption tower, an outlet of the high-pressure absorption tower is connected with a regeneration tower, and a shell side outlet of the heat recovery heat exchanger is connected with a reboiler at the bottom of the regeneration tower.
Further, a material outlet at the bottom of the evaporator is connected with a material inlet of the reaction kettle.
Further, a liquid phase material outlet at the bottom of the light component removal tower is connected with an evaporator.
Further, a liquid-phase material outlet is formed in the side wall of the lower portion of the finished product tower and connected with the stripping tower. Further separating the heavy component impurities.
Furthermore, a stripping tower preheating reboiler and a stripping tower bottom reboiler are sequentially connected in series at the bottom of the stripping tower, a shell pass outlet of the heat recovery heat exchanger is connected with the stripping tower preheating reboiler, and the stripping tower bottom reboiler is connected with a boiler steam source. The energy consumption for separating heavy component impurities is reduced.
The utility model has the advantages that:
the utility model discloses an increase the heat recovery heat exchanger, the selection to the heat transfer fluid route, the interpolation of power cycle pump and back pressure valve, thereby utilize the saturated steam of reaction heat production 0.6 ~ 0.8MPa (G) among the synthetic acetic acid reaction process, this steam of having retrieved can provide the heat to all rectifying column in the technology, and can provide whole heats to its part rectifying column (lightness-removing column, dealkylation tower, regenerator column etc.), greatly reduced former technology to the consumption of steam total amount, reduce the energy consumption of methyl alcohol low pressure carbonyl synthetic acetic acid technology, reduce the waste of the energy.
Drawings
The accompanying drawings, which form a part of the specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without unduly limiting the scope of the invention.
FIG. 1 is a schematic structural diagram of a system for low-pressure methanol oxo-synthesis of acetic acid with recycled reaction heat according to embodiment 1 of the present invention;
wherein, 1, a reaction kettle, 2, an evaporator, 3, a light component removal tower, 4, a dehydration tower, 5, a finished product tower, 6, a stripping tower, 7, a delayer, 8, a dealkylation tower, 9, a low-pressure absorption tower, 10, a high-pressure absorption tower, 11, a regeneration tower, 12, a heat recovery heat exchanger, 13, a regeneration tower reboiler, 14, a light component removal tower reboiler, 15, a dealkylation tower reboiler, 16, a tower bottom reboiler of the dehydration tower, 17, a dehydration tower preheating reboiler, 18, a tower bottom reboiler of the finished product tower, 19, a finished product tower preheating reboiler, 20, a tower bottom reboiler of the stripping tower, 21, and a stripping tower preheating reboiler.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
In order to make the technical solutions of the present invention more clearly understood by those skilled in the art, the technical solutions of the present invention will be described in detail below with reference to specific embodiments.
Example 1
A system for synthesizing acetic acid by methanol low-pressure carbonyl with reaction heat recycling is shown in figure 1 and comprises a methanol low-pressure carbonyl synthesis acetic acid system, a heat recovery heat exchanger 12, a dehydration tower preheating reboiler 17, a finished product tower preheating reboiler 19 and a stripping tower preheating reboiler 21.
The methanol low-pressure oxo-synthesis acetic acid system comprises a reaction kettle 1, an evaporator 2, a light component removal tower 3, a dehydration tower 4 and a finished product tower 5. A liquid-phase product outlet of the reaction kettle is connected with a material inlet of the evaporator 2, a gas-phase outlet of the evaporator 2 is connected with a light component removal tower, a product outlet of the light component removal tower 3 is connected with a material inlet of the dehydration tower 4, a tower bottom product outlet of the dehydration tower 4 is connected with a material inlet of the finished product tower 5, and a product outlet of the finished product tower 5 is connected with a product condenser. The tower bottom liquid phase material outlet of the finished product tower 5 is connected with the material inlet of the stripping tower 6.
The gas phase outlet of the light component removing tower 3 is connected with the inlet of a condenser at the top of the light component removing tower, the outlet of the condenser at the top of the light component removing tower is connected with a delayer 7, the bottom outlet of the delayer 7 is connected with a dealkylation tower 8, the top outlet of the delayer 7 is connected with a low-pressure absorption tower 9, and the outlet of the low-pressure absorption tower 9 is connected with a regeneration tower 11. The middle outlet of the delayer 7 is connected with the upper inlet of the lightness-removing column 3. The liquid phase material outlet at the bottom of the light component removal tower 3 is connected with the evaporator 2.
The gas phase outlet of the reaction kettle 1 is connected with the inlet of a high-pressure absorption tower 10, and the outlet of the high-pressure absorption tower 10 is connected with a regeneration tower 11.
The material outlet at the bottom of the evaporator 2 is connected with the material inlet of the reaction kettle 1.
The tower bottom of the dehydration tower 4 is provided with a dehydration tower pre-heating reboiler 17 and a dehydration tower bottom reboiler 16 in sequence according to the circulating liquid phase direction.
And a finished product tower preheating reboiler 19 and a finished product tower bottom reboiler 18 are sequentially arranged at the bottom of the finished product tower 5 according to the circulating liquid phase direction.
At the bottom of the stripping tower 6, a stripping tower pre-heating reboiler 21 and a stripping tower bottom reboiler 20 are sequentially installed according to the circulating liquid phase direction.
The heat recovery heat exchanger 12 is a shell-and-tube heat exchanger, a tube side inlet of the heat recovery heat exchanger 12 is connected with an outlet of a power circulating pump, an inlet of the power circulating pump is connected with a reaction liquid outlet of the reaction kettle 1, a tube side outlet of the heat recovery heat exchanger 12 is connected with a reaction liquid inlet of the reaction kettle 1, a shell side inlet of the heat recovery heat exchanger 12 is connected with a boiler water outlet, a shell side outlet of the heat recovery heat exchanger 12 is connected with a regeneration tower reboiler 13, a light component removal tower reboiler 14, a dealkylation tower reboiler 15, a dehydration tower preheating reboiler 17, a finished product tower preheating reboiler 19, a stripping tower preheating reboiler 21, and a pipeline of a shell side outlet of the heat recovery heat exchanger 12 is provided with a back pressure valve.
The bottom reboiler 16 of the dehydrating tower, the bottom reboiler 18 of the finished product tower and the bottom reboiler 20 of the stripping tower are connected with a boiler steam source (1.3 MPa).
The technical raw materials of the acetic acid synthesis process by methanol low-pressure carbonyl are that methanol and carbon monoxide react in a reaction kettle under the action of a catalyst and under a certain condition to generate acetic acid; the reacted gas phase material flow enters a high-pressure absorption tower, components such as promoter methyl iodide and the like in tail gas are absorbed by methanol, and the reacted liquid phase material flow enters an evaporator for flash evaporation separation; the liquid phase after flash evaporation mainly comprises acetic acid, main catalyst and other material flows which return to the reaction kettle to continue to take part in the reaction, and the gas phase after flash evaporation mainly comprises acetic acid, methyl acetate, water, cocatalyst and other material flows which enter the light component removal tower. Removing light components such as promoter methyl iodide and the like through the rectification operation of a light component removal tower, and removing the multi-carbon alkane in the system through a dealkylation tower; the tail gas of the light component removal tower enters a low-pressure absorption tower, methanol is used for absorbing components such as cocatalyst methyl iodide in the tail gas, and the crude acetic acid separated by the light component removal tower enters a dehydration tower for dehydration; and (3) after the dehydrated dry acetic acid is extracted from the tower kettle of the dehydration tower, the dry acetic acid enters a finished product tower for purification and rectification, and is matched with a stripping tower to remove propionic acid impurities in the system. The regeneration tower is used for regenerating methyl iodide.
The heat generation process is as follows: raw materials of methanol and carbon monoxide react in a reaction kettle under the action of a catalyst and a cocatalyst by controlling certain pressure and temperature to generate acetic acid, and heat is released in the reaction process.
The reaction heat recovery process comprises the following steps: 192 ℃ high-temperature reaction liquid flows out of the middle of the reaction kettle, enters a heat recovery heat exchanger after being pressurized by a power circulating pump, the shell pass of the heat recovery heat exchanger is high-temperature boiler water, the tube pass of the heat recovery heat exchanger is high-temperature reaction liquid, two material partition wall heat exchange is carried out, part of the high-temperature boiler water is vaporized into 0.6-0.8 MPa (G) saturated steam, the steam temperature is 158-175 ℃, the high-temperature boiler water is recycled and applied to each rectifying tower to heat the steam or is used for a power generation device, and the high-temperature reaction liquid returns to the reaction kettle from the upper part of the reaction kettle after the temperature of the high-temperature reaction liquid is reduced to continue to participate in the reaction. Because the initial temperature of the high-temperature reaction liquid and the pressure of the byproduct steam are limited, the flow rate of the high-temperature reaction liquid determines the reaction heat recovery efficiency, one set of heat recovery device can be arranged for a small reaction kettle, and two or more sets of heat recovery devices can be arranged for a large reaction kettle under the condition of higher production load, so that the heat recovery efficiency is higher, and the available steam grade is wider.
The recycling process of the recovered heat comprises the following steps: the kettle temperature control of the light component removal tower, the dealkylation tower and the regeneration tower is low, 0.6-0.8 MPa (G) saturated steam which is a byproduct of reaction heat can be directly used, and the temperature control indexes are as follows: the temperature index of the light component removal tower kettle is 128-134 ℃, the temperature index of the dealkylation tower kettle is 138-145 ℃, and the temperature index of the regeneration tower kettle is 90-92 ℃. The power generation apparatus also directly generates power by using the byproduct steam. The temperature control of the kettle of the dehydration tower, the finished product tower and the stripping tower is high, the byproduct steam can not meet the rectification separation requirement, two reboilers are required to be connected in series, the temperature is firstly raised to 125-145 ℃ by the aid of the byproduct steam through a first reboiler, then the temperature is continuously heated to a proper temperature by the aid of 1.3MPa steam through a second reboiler, and the temperature control indexes are as follows: the temperature index of the dehydration tower kettle is 156-159 ℃, the temperature index of the finished product tower kettle is 145-150 ℃, and the temperature index of the stripping tower kettle is 156-158 ℃.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for synthesizing acetic acid by methanol low-pressure carbonyl with reaction heat recycling is characterized by comprising a reaction kettle, an evaporator, a light component removal tower, a dehydration tower and a finished product tower;
the reaction kettle is provided with a reaction liquid outlet, a reaction liquid inlet and a product outlet, a power circulating pump and a heat recovery heat exchanger are sequentially connected between the reaction liquid outlet and the reaction liquid inlet, the heat recovery heat exchanger is a shell-and-tube heat exchanger, the reaction liquid inlet is communicated with the tube side of the heat recovery heat exchanger, the shell side of the heat recovery heat exchanger is communicated with a boiler water outlet, and the product outlet of the reaction kettle is connected with an evaporator;
a gas phase outlet of the evaporator is connected with a light component removal tower, a gas phase outlet is formed in the top of the light component removal tower, a product outlet is formed in the middle of the light component removal tower, the gas phase outlet of the light component removal tower is connected with a dealkylation tower, and the product outlet of the light component removal tower is connected with a dehydration tower;
the bottom of the dehydration tower is sequentially connected in series with a dehydration tower preheating reboiler and a tower bottom reboiler of the dehydration tower, the bottom of the dehydration tower is provided with a product outlet, and the product outlet of the dehydration tower is connected with a finished product tower;
the bottom of the finished product tower is sequentially connected in series with a finished product tower preheating reboiler and a finished product tower bottom reboiler;
the shell pass outlet of the heat recovery heat exchanger is connected with a lightness-removing tower reboiler, a dehydration tower preheating reboiler and a finished product tower preheating reboiler, and a pipeline of the shell pass outlet of the heat recovery heat exchanger is provided with a back pressure valve;
the tower bottom reboiler of the dehydration tower and the tower bottom reboiler of the finished product tower are connected with a boiler steam source.
2. The system for low-pressure carbonylation of methanol to acetic acid with recovery of reaction heat as claimed in claim 1, wherein the gas phase outlet of the lightness-removing column is connected to the inlet of the condenser at the top of the lightness-removing column, the outlet of the condenser at the top of the lightness-removing column is connected to the dealkylation column, and the shell-side outlet of the heat recovery exchanger is connected to the reboiler at the bottom of the dealkylation column.
3. The system for the low-pressure oxo synthesis of acetic acid from methanol by recycling the reaction heat as claimed in claim 2, wherein the outlet of the condenser at the top of the light component removal tower is connected with a demixer, and the outlet at the bottom of the demixer is connected with the dealkylation tower.
4. The system for low-pressure carbonylation of methanol to acetic acid with recovery of reaction heat as claimed in claim 3, wherein the top outlet of the layering device is connected to the low-pressure absorption tower, the outlet of the low-pressure absorption tower is connected to the regeneration tower, and the shell-side outlet of the heat recovery heat exchanger is connected to the reboiler at the bottom of the regeneration tower.
5. The system for the low-pressure oxo synthesis of acetic acid from methanol by recycling the heat of reaction as claimed in claim 3, wherein the middle outlet of the delayer is connected to the upper inlet of the lightness-removing column.
6. The system for low-pressure oxo synthesis of acetic acid from methanol by recycling of reaction heat as claimed in claim 1, wherein the gas phase outlet of the reaction kettle is connected with the inlet of the high-pressure absorption tower, the outlet of the high-pressure absorption tower is connected with the regeneration tower, and the shell side outlet of the heat recovery heat exchanger is connected with the reboiler at the bottom of the regeneration tower.
7. The system for low-pressure carbonylation of methanol to acetic acid with recovery of reaction heat as claimed in claim 1, wherein the bottom material outlet of the evaporator is connected to the material inlet of the reaction vessel.
8. The system for the low-pressure oxo synthesis of acetic acid from methanol by recycling the heat of reaction according to claim 1, wherein the liquid material outlet at the bottom of the light component removal column is connected to an evaporator.
9. The system for the low-pressure oxo synthesis of acetic acid from methanol by recycling the reaction heat as claimed in claim 1, wherein the side wall of the lower part of the finished product tower is provided with a liquid-phase material outlet, and the liquid-phase material outlet is connected with the stripping tower.
10. The system for low-pressure oxo synthesis of acetic acid from methanol by recycling of reaction heat as claimed in claim 9, wherein the bottom of the stripping column is sequentially connected in series with a stripping column pre-heating reboiler and a stripping column bottom reboiler, the shell side outlet of the heat recovery heat exchanger is connected with the stripping column pre-heating reboiler, and the stripping column bottom reboiler is connected with the boiler steam source.
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