CN117753029A - Purification device and purification process - Google Patents
Purification device and purification process Download PDFInfo
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- CN117753029A CN117753029A CN202311591408.6A CN202311591408A CN117753029A CN 117753029 A CN117753029 A CN 117753029A CN 202311591408 A CN202311591408 A CN 202311591408A CN 117753029 A CN117753029 A CN 117753029A
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- 238000000746 purification Methods 0.000 title claims abstract description 67
- 238000010521 absorption reaction Methods 0.000 claims abstract description 176
- 238000001816 cooling Methods 0.000 claims abstract description 77
- 238000006243 chemical reaction Methods 0.000 claims abstract description 64
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 35
- 239000000047 product Substances 0.000 claims description 249
- 239000007791 liquid phase Substances 0.000 claims description 121
- 238000000926 separation method Methods 0.000 claims description 112
- 239000007795 chemical reaction product Substances 0.000 claims description 70
- 239000012071 phase Substances 0.000 claims description 57
- 239000012263 liquid product Substances 0.000 claims description 52
- 238000010574 gas phase reaction Methods 0.000 claims description 33
- 238000000034 method Methods 0.000 claims description 26
- 239000006096 absorbing agent Substances 0.000 claims description 21
- 230000008569 process Effects 0.000 claims description 19
- 230000002745 absorbent Effects 0.000 claims description 16
- 239000002250 absorbent Substances 0.000 claims description 16
- 239000006227 byproduct Substances 0.000 claims description 13
- 239000000110 cooling liquid Substances 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 2
- 230000000712 assembly Effects 0.000 claims 1
- 238000000429 assembly Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000001311 chemical methods and process Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 88
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 65
- 230000000052 comparative effect Effects 0.000 description 41
- 239000001257 hydrogen Substances 0.000 description 40
- 229910052739 hydrogen Inorganic materials 0.000 description 40
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 34
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 31
- 239000007788 liquid Substances 0.000 description 29
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 16
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 12
- 230000006835 compression Effects 0.000 description 10
- 238000007906 compression Methods 0.000 description 10
- 235000010290 biphenyl Nutrition 0.000 description 8
- 239000004305 biphenyl Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- WIRUZQNBHNAMAB-UHFFFAOYSA-N benzene;cyclohexane Chemical compound C1CCCCC1.C1=CC=CC=C1 WIRUZQNBHNAMAB-UHFFFAOYSA-N 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 6
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 6
- 238000005984 hydrogenation reaction Methods 0.000 description 6
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 6
- 239000012808 vapor phase Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 3
- XIVQMBJJCVVPCF-UHFFFAOYSA-N methylcyclohexane;toluene Chemical compound CC1CCCCC1.CC1=CC=CC=C1 XIVQMBJJCVVPCF-UHFFFAOYSA-N 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000001737 promoting effect Effects 0.000 description 3
- 239000012495 reaction gas Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 description 2
- UJOBWOGCFQCDNV-UHFFFAOYSA-N 9H-carbazole Chemical compound C1=CC=C2C3=CC=CC=C3NC2=C1 UJOBWOGCFQCDNV-UHFFFAOYSA-N 0.000 description 2
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- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- ZRJUCHNILNOEKV-UHFFFAOYSA-N hexan-2-one hydrate Chemical compound O.CCCCC(C)=O ZRJUCHNILNOEKV-UHFFFAOYSA-N 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
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- PXXNTAGJWPJAGM-UHFFFAOYSA-N vertaline Natural products C1C2C=3C=C(OC)C(OC)=CC=3OC(C=C3)=CC=C3CCC(=O)OC1CC1N2CCCC1 PXXNTAGJWPJAGM-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a purification device and a purification process, relates to the technical field of chemical processes and equipment, and aims to solve the problem of high energy consumption during purification of dehydrogenation products. The device comprises: the reaction unit, the stripping tower that is connected with the reaction unit, the absorption tower that is connected with the stripping tower, the cooling unit that is connected with the absorption tower. The purification process is applied to the purification device provided by the technical scheme. The purification device provided by the invention is used for purifying the dehydrogenation product.
Description
Technical Field
The invention relates to the technical field of chemical technology and equipment, in particular to a purification device and a purification technology.
Background
The hydrogen storage of the organic liquid is realized by hydrogenation and dehydrogenation of specific liquid and hydrogen under the action of a catalyst. However, a small amount of heavy components are generated in the hydrogenation and dehydrogenation reaction processes, and the continuous accumulation of a small amount of heavy components can lead to catalyst poisoning and increase of pressure drop of a reactor, so that the conversion rate of the reaction is affected. Therefore, purification of the dehydrogenation product is required. However, the energy consumption required in the purification process of the current dehydrogenation product is larger, the energy-saving requirement is not met, and the cost of hydrogen storage is increased.
Disclosure of Invention
The invention aims to provide a purification device and a purification process, which are used for purifying a dehydrogenation product.
In order to achieve the above object, the present invention provides the following technical solutions:
a purification apparatus for purification of a dehydrogenation product, the apparatus comprising:
a reaction unit for obtaining a gas phase reaction product and a liquid phase reaction product;
the stripping tower is connected with the reaction unit and is used for separating a liquid phase reaction product sent into the stripping tower by the reaction unit to obtain a stripping gas phase product and a stripping liquid phase product, wherein the stripping liquid phase product is a reaction byproduct;
the absorption tower is connected with the stripping tower and is used for carrying out absorption separation on the stripping gas-phase product sent into the absorption tower by the stripping tower and the gas-phase reaction product sent into the absorption tower to obtain an absorption gas-phase product and an absorption liquid-phase product;
and the cooling unit is connected with the absorption tower and is used for cooling the absorption gas-phase product sent into the cooling unit by the absorption tower to obtain a gas product and a liquid product.
Compared with the prior art, in the purification device provided by the invention, the gas-phase reaction product generated by the reaction unit is directly sent into the absorption tower through the top of the stripping tower for absorption and separation, and the liquid-phase reaction product generated by the reaction unit is sent into the stripping tower for separation, so that only the liquid-phase reaction product obtained by the reaction of the reaction unit is required to be treated in the stripping tower, the workload of the stripping tower is greatly reduced, and the steam amount required by the stripping tower in the treatment process is smaller, thereby being more energy-saving and environment-friendly. Meanwhile, the stripping gas phase product obtained by separating the gas phase reaction product and the stripping tower is sent into an absorption tower for absorption and separation, and the gas phase reaction product and the stripping gas phase product are further purified by the absorption tower, so that less byproducts are contained in the gas in the absorption gas phase product sent into a cooling unit through the absorption tower, and the purity of the finally obtained gas product and liquid product is improved.
The invention also provides a purification process, which is applied to the purification device and comprises the following steps:
sending a gas phase reaction product and a liquid phase reaction product generated by a reaction unit into a stripping tower, and separating the liquid phase reaction product by using the stripping tower to obtain a stripping gas phase product and a stripping liquid phase product, wherein the stripping liquid phase product is a reaction byproduct;
sending the stripping gas-phase product and the gas-phase reaction product into an absorption tower for absorption and separation to obtain an absorption gas-phase product and an absorption liquid-phase product;
and sending the gas-phase product to the cooling unit for cooling to obtain a gas product and a liquid product.
Compared with the prior art, the purification process provided by the invention has the same beneficial effects as the purification device in the technical scheme, and the description is omitted here.
Drawings
The accompanying drawings, which 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 and do not constitute a limitation on the invention. In the drawings:
fig. 1 shows a schematic structural view of a purifying apparatus according to an exemplary embodiment of the present invention;
Fig. 2 shows a second schematic structural view of the purifying apparatus according to the exemplary embodiment of the present invention;
FIG. 3 illustrates a flow chart one of a purification process provided in accordance with an exemplary embodiment of the present invention;
FIG. 4 illustrates a second flow chart of a purification process provided in accordance with an exemplary embodiment of the present invention;
FIG. 5 illustrates a third flow chart of a purification process provided in accordance with an exemplary embodiment of the present invention;
FIG. 6 illustrates a fourth flow chart of a purification process provided in accordance with an exemplary embodiment of the present invention;
FIG. 7 illustrates a fifth flow chart of a purification process provided in accordance with an exemplary embodiment of the present invention;
fig. 8 is a schematic view showing the structure of a conventional purifying apparatus according to an exemplary embodiment of the present invention.
Reference numerals:
151-a raw material pump, 152-a heat exchanger;
153-reactor, 154-stripping column;
155-reboiler, 156-absorption tower;
157-cooling assembly, 158-separator tank;
159-a circulation pump, 160-a cooler;
161-compressor, 162-product coarse separator tank;
551-raw material pump of comparative example, 552-heat exchanger of comparative example;
553-comparative example reactor, 554-comparative example first product knockout drum;
555-comparative cooler, 556-comparative second product separator tank;
557-rectifying column of comparative example, 558-reboiler of comparative example;
559-overhead condenser of comparative example, 560-overhead reflux drum of comparative example;
561-comparative compressor.
Detailed Description
Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings. It should be understood that the description is only illustrative and is not intended to limit the scope of the invention. In addition, in the following description, descriptions of well-known structures and techniques are omitted so as not to unnecessarily obscure the present invention.
Various structural schematic diagrams according to embodiments of the present invention are shown in the accompanying drawings. The figures are not drawn to scale, wherein certain details are exaggerated for clarity of presentation and may have been omitted. The shapes of the various regions, layers and relative sizes, positional relationships between them shown in the drawings are merely exemplary, may in practice deviate due to manufacturing tolerances or technical limitations, and one skilled in the art may additionally design regions/layers having different shapes, sizes, relative positions as actually required.
In the context of the present invention, when a layer/element is referred to as being "on" another layer/element, it can be directly on the other layer/element or intervening layers/elements may be present therebetween. In addition, if one layer/element is located "on" another layer/element in one orientation, that layer/element may be located "under" the other layer/element when the orientation is turned. In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. The meaning of "a number" is one or more than one unless specifically defined otherwise.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The various devices and components of the present invention are commercially available and will not be described in further detail below.
In the new energy system, compared with other energy sources, the hydrogen energy has high heat value, and the combustion product is only water, so that the method is the most environment-friendly and ideal secondary energy source. Hydrogen is therefore considered to be the most promising energy carrier to replace traditional fossil fuels.
Currently, the bottleneck of large-scale application of hydrogen is that hydrogen energy is difficult to efficiently and safely store and transport. The hydrogen storage of organic liquid is an emerging technology of hydrogen storage realized by respectively carrying out hydrogenation and dehydrogenation reactions on specific liquid (such as methylcyclohexane, cyclohexane, carbazole, decalin and the like) and hydrogen under the action of a catalyst. Organic liquid hydrogen storage systems offer the following advantages over other hydrogen storage systems: 1. the hydrogen storage density is high; 2. the safety coefficient of the hydrogen storage system in the transportation process is high; 3. the reactant is stable, and can be recycled for a plurality of times. Thus, organic liquid hydrogen storage systems are considered as an effective means of enabling large scale hydrogen energy storage, remote hydrogen energy transport and replacement of traditional fossil fuels.
But during the hydrogenation and dehydrogenation reactions of the organic liquid hydrogen storage, small amounts of heavy components (e.g., biphenyl, methylnaphthalene, etc.) are produced. In the following, a hydrogen storage scheme using a methylcyclohexane-toluene system and a cyclohexane-benzene system as hydrogen storage media will be described as an example, and for the hydrogen storage scheme using a methylcyclohexane-toluene system and a cyclohexane-benzene system as hydrogen storage media, repeated use of hydrogenation and dehydrogenation liquid products can lead to continuous accumulation of heavy components, thereby blocking the active space of a hydrogenation catalyst and a dehydrogenation catalyst, and causing disadvantages of catalyst poisoning and increased pressure drop of a reactor. Besides being used as a hydrogen storage medium, the cyclohexane-benzene system can be used as raw materials of water and a process for preparing cyclohexanone by using benzene and hydrogen produced by dehydrogenating cyclohexane, so that the utilization rate of benzene is increased. However, the content of heavy components contained in benzene in the water and cyclohexanone process is extremely high, so that the heavy components such as biphenyl in benzene must be removed by a proper means to meet the production requirements of the water and cyclohexanone process and improve the utilization rate of benzene.
However, when the dehydrogenation product is purified by using the conventional process, the heat required in the stripping stage is large, so that the cost is high, and the requirements of energy conservation and environmental protection are not met.
In order to overcome the problems, the exemplary embodiment of the invention provides a purifying device for purifying a dehydrogenation product, so as to solve the problems that the heat consumption is overlarge, the cost is high and the energy-saving and environment-friendly requirements are not met when the dehydrogenation product is purified.
Fig. 1 shows a schematic structural diagram of a purifying apparatus according to an exemplary embodiment of the present invention, and as shown in fig. 1, the purifying apparatus according to an exemplary embodiment of the present invention includes:
and a reaction unit for obtaining a gas phase reaction product and a liquid phase reaction product. For example, in the case of cyclohexane-benzene system, when cyclohexane is fed into a reaction unit for dehydrogenation, the gas phase reaction product obtained is hydrogen, and the liquid phase reaction product obtained is benzene and heavy components (reaction by-products such as biphenyl, etc.).
In practical applications, the reaction unit may include a heat exchanger 152 and a reactor 153. The cyclohexane-benzene system will be described below as an example. Cyclohexane and a part of the dehydrogenation gas product can be mixed and sent into the heat exchanger 152 for heat exchange, so that the cyclohexane is heated and vaporized, and the cyclohexane and the dehydrogenation gas product are mixed to form mixed gas. The heat exchange temperature in the heat exchanger 152 is 40-90 ℃. For example, the heat exchange temperature may be 40 ℃, 50 ℃, 70 ℃, 90 ℃, or the like, but is not limited thereto. Then, the mixed gas is heated and then fed into a reactor 153 for cyclohexane dehydrogenation reaction, so as to obtain a gas-phase reaction product and a liquid-phase reaction product. The reaction conditions may include: the reaction temperature is 250-400 ℃ and the reaction pressure is 1kg/cm 2 ～5kg/cm 2 . For example, the reaction temperature may be 250 ℃, 320 ℃, 350 ℃, 400 ℃, or the like, but is not limited thereto. The reaction pressure may be 1kg/cm 2 、2kg/cm 2 、3kg/cm 2 、4kg/cm 2 Or 5kg/cm 2 And the like, without being limited thereto. The heating temperature of the mixed gas can be 280-360 ℃. For example, the heating temperature may be 280 ℃, 320 ℃, 360 ℃ or the like, but is not limited thereto. Wherein cyclohexane may be pressurized by feed pump 151 and mixed with the dehydrogenation gas product.
And a stripping tower 154 connected with the reaction unit and used for separating the liquid phase reaction product sent into the stripping tower 154 by the reaction unit to obtain a stripping gas phase product and a stripping liquid phase product, wherein the stripping liquid phase product is a reaction byproduct. Because the boiling point of the heavy component is higher, the liquid phase reaction product is sent into the stripping tower 154 for separation, the obtained stripping gas phase product can comprise benzene, cyclohexane and a small amount of components, and the like, so that the stripping liquid phase product is obtained as the heavy component, namely a reaction byproduct, and at the moment, the heavy component at the bottom of the stripping tower 154 can be directly discharged and collected. The reaction conditions of stripping column 154 may include: the temperature of the top of the stripping tower 154 is 50-55 ℃, the temperature of the tower kettle is 180-220 ℃ and the pressure is 0.1-5 barG. For example, the top temperature of the stripping column 154 may be 50 ℃, 52 ℃, 55 ℃, or the like, but is not limited thereto. The temperature of the tower bottom can be 180 ℃, 200 ℃ or 220 ℃ and the like, but is not limited to the above. The pressure may be 0.1barG, 0.5barG, 2barG, 5barG, etc., and is not limited thereto. A reboiler 155 for supplying heat to heat the benzene in the liquid phase and convert it into benzene in the gas phase is connected to the bottom of the stripping column 154, and the benzene is fed into the stripping column 154 to be separated.
In practical applications, before the gas-phase reaction product and the liquid-phase reaction product of the reaction unit are sent to the stripping tower 154, the gas-phase reaction product and the liquid-phase reaction product may be sent to the heat exchanger 152 for heat exchange and cooling, and then the cooled gas-phase reaction product and the cooled liquid-phase reaction product are sent to the stripping tower 154 for separation, so that heavy components of a part of gas phase can be converted into liquid phase, and the content of heavy components in the gas-phase reaction product is reduced. The cooling temperature may be 50℃to 90 ℃. For example, the cooling temperature may be 50 ℃, 60 ℃, 70 ℃, 90 ℃ or the like, but is not limited thereto.
And an absorption tower 156 connected with the stripping tower 154, and is used for carrying out absorption separation on the stripped gas-phase product sent into the absorption tower 156 by the stripping tower 154 and the gas-phase reaction product sent into the absorption tower 156 to obtain an absorption gas-phase product and an absorption liquid-phase product. The stripping gas phase product sent from the stripping tower 154 into the absorption tower 156 and the gas phase reaction product sent into the absorption tower 156 are absorbed and separated by the absorption tower 156 connected with the stripping tower 154, so that the obtained gas product and liquid product have lower heavy component content.
And a cooling unit connected to the absorption tower 156 for cooling the absorption gas phase product fed into the cooling unit by the absorption tower 156 to obtain a gas product and a liquid product. The gas product and the liquid product are further separated by the cooling unit, so that a gas product and a liquid product having a higher purity can be obtained. The gas product with the volume flow rate of 10% -30% in the gas product is used as the reaction gas to be sent into the reaction unit, and the rest gas products are directly output.
According to the purification device provided by the invention, the gas-phase reaction product generated by the reaction unit is directly sent into the absorption tower through the top of the stripping tower for absorption and separation, and the liquid-phase reaction product generated by the reaction unit is sent into the stripping tower for separation, so that only the liquid-phase reaction product obtained by the reaction of the reaction unit is required to be treated in the stripping tower, the workload of the stripping tower is greatly reduced, and the steam amount required by the stripping tower in the treatment process is smaller, thereby being more energy-saving and environment-friendly. Meanwhile, the stripping gas phase product obtained by separating the gas phase reaction product and the stripping tower is sent into an absorption tower for absorption and separation, and the gas phase reaction product and the stripping gas phase product are further purified by the absorption tower, so that less byproducts are contained in the gas in the absorption gas phase product sent into a cooling unit through the absorption tower, and the purity of the finally obtained gas product and liquid product is improved.
As a possible implementation manner, fig. 2 shows a schematic structural diagram of a purifying apparatus according to an exemplary embodiment of the present invention. As shown in fig. 2, the apparatus may further include a product crude separation tank 162 connected to the reaction unit and the stripping column 154, respectively, for crude separation of the gas phase reaction product and the liquid phase reaction product to obtain a crude gas phase product and a crude liquid phase product before the stripping column 154 separates the liquid phase reaction product fed into the stripping column 154 from the reaction unit. The stripping column 154 is used to separate the crude liquid phase product from the product crude knockout drum 162 fed to the stripping column 154 by feeding the crude liquid phase product to the stripping column 154. The absorber 156 is connected to the product crude separation tank 162 for absorbing and separating the crude separated vapor phase product and the stripped vapor phase product from the product crude separation tank 162 fed to the absorber 156 by feeding the crude separated vapor phase product to the absorber 156. By arranging the product crude separation tank 162 between the reaction unit and the stripping tower 154, after the gas-phase reaction product and the liquid-phase reaction product obtained in the reaction unit can be subjected to crude separation in the product crude separation tank 162, the crude separation gas-phase product at the top of the product crude separation tank 162 is sent into the absorption tower 156, and the crude separation liquid-phase product at the bottom of the product crude separation tank 162 is sent into the stripping tower 154, so that the amount of the crude separation liquid-phase product sent into the stripping tower 154 is further reduced, the treatment amount of the stripping tower 154 is reduced, and the steam amount is reduced, so that the purification device provided by the exemplary embodiment of the invention is more energy-saving and environment-friendly.
As a possible implementation, as shown in fig. 1 and 2, the apparatus may further include a circulating cooling unit connected to the absorption tower 156 for cooling the absorption liquid-phase product. So that the cooled absorption liquid phase product is fed into the absorption tower 156 again, the absorption liquid phase product can act as an absorbent on the gas in the absorption tower 156, and the temperature gradient is generated in the absorption tower 156 by continuously feeding the cooled absorption liquid phase product into the absorption tower 156 through the circulating cooling unit due to the temperature difference between the cooled absorption liquid phase product and the gas in the absorption tower 156, thereby promoting absorption, and further reducing the content of heavy components contained in the absorption gas phase product finally obtained at the top of the absorption tower 156.
As a possible implementation, as shown in fig. 1 and 2, the above-mentioned circulating cooling unit is further connected to the stripping column 154, and is used for sending the absorption liquid-phase product with the mass flow rate of 5% -25% into the stripping column 154 for separation. So that the absorption liquid product at the bottom of the absorption column 156 can be continuously fed into the stripping column 154 for separation, and further heavy components in the absorption liquid product are separated.
In some alternatives, as shown in fig. 1 and 2, the above-described circulation cooling unit may include a circulation pump 159 and a cooler 160.
As shown in fig. 1 and 2, the above-mentioned circulating pump 159 is connected to the absorption column 156 for withdrawing the absorption liquid-phase product in the absorption column 156, so that the absorption liquid-phase product in the absorption column 156 can be circulated to the upper middle portion of the absorption column 156 and introduced into the absorption column 156 as an absorption liquid.
As shown in fig. 1 and 2, the circulating pump 159 is connected to the stripping tower 154, and is used for sending the absorption liquid phase product with the mass flow rate of 5% -25% in the absorption liquid phase product pumped by the circulating pump 159 into the stripping tower 154 for separation, so as to remove heavy components in the absorption liquid phase product, and the heavy components in the absorption liquid phase product finally flow out from the bottom of the stripping tower 154 as reaction byproducts. It is to be understood that the mass flow rate herein may be 5%, 10%, 15%, 20%, 25%, etc., and is not limited thereto.
As shown in fig. 1 and 2, the cooler 160 is connected to the circulating pump 159, and is configured to cool the absorption liquid product pumped by the circulating pump 159, and send the cooled absorption liquid product into the absorption tower 156 as an absorbent, so as to generate a temperature gradient in the absorption tower 156, thereby improving absorption efficiency, and further reducing heavy components in the absorption gas phase product in the absorption tower 156, so that the content of heavy components in the finally obtained liquid product is less than 1PPM.
As a possible implementation, as shown in fig. 1 and 2, the cooling unit may include: at least one cooling separation module is coupled to the absorber 156 for cooling separation of the absorbed vapor phase product from the absorber 156 fed to the cooling separation module to obtain a cooled gas product and a cooled liquid product.
In practice, as shown in fig. 1 and 2, the at least one cooling separation assembly may include a cooling assembly 157 and a separation tank 158, where the cooling assembly 157 may be a cooler for cooling the absorbent gas-phase product to condense a portion of the components in the absorbent gas-phase product into a liquid to separate the gas product and the liquid product in the absorbent gas-phase product.
A compressor 161 coupled to the at least one cooling separation module for pressure separation of the cooled gas product to obtain a gas product and a pressurized liquid product, wherein the liquid product may comprise the cooled liquid product and the pressurized liquid product at a mass flow rate of 80% to 100%. It is to be understood that the mass flow rate herein may be 80%, 85%, 90%, 97% or 100%, etc., and is not limited thereto.
At least one cooling separation module is also coupled to the absorber tower 156 for delivering a cooling liquid product having a mass flow rate of 0% to 20% as an absorbent into the absorber tower 156. It is to be understood that the mass flow rate herein may be 0%, 5%, 10%, 15%, 20%, etc., and is not limited thereto. Because the purity of the cooled liquid product is high, by feeding the cooled liquid product with a mass flow rate of 0% to 20% into the absorption tower 156 as an absorbent, a concentration gradient is formed in the absorption tower 156, thereby promoting the absorption of heavy components in the gas in the absorption tower 156, improving the absorption efficiency, and further reducing the content of heavy components in the absorbed gas phase product, so that the content of heavy components in the finally obtained liquid product is less than 1PPM.
In practice, as shown in fig. 1 and 2, the cooling separation assembly may include a cooler and a separation tank 158, wherein the cooler is connected to the absorption tower 156, and is configured to cool the absorption gas-phase product sent from the absorption tower 156 into the cooler, so as to obtain a cooled gas-phase product and a cooled liquid-phase product; a separator tank 158 is connected to the cooler for gas-liquid separation of the cooled gas phase product and the cooled liquid phase product to obtain a separated gas phase product and a separated liquid phase product. The separated vapor phase product may be fed to a compressor 161 for pressurized separation and the separated liquid phase product may be output as a liquid product. Of course, in order to increase the absorption efficiency of the absorption tower 156, a separated liquid-phase product having a mass flow rate of 80% to 100% may be fed into the absorption tower 156 as an absorbent. It is to be understood that the mass flow rate herein may be 80%, 85%, 90%, 97% or 100%, etc., and is not limited thereto.
For example, to increase the purity of the liquid product, the purification device may include a plurality of cooling separation modules, in which case the plurality of cooling separation modules may be connected together in series. And taking the gas product separated by the last cooling separation assembly as a cooling gas product, and taking the liquid product separated as a cooling liquid product.
The embodiment of the invention also provides a purification process which can be applied to the purification device provided by the exemplary embodiment of the invention to purify the dehydrogenation product and reduce the heat consumption of the purification of the dehydrogenation product, so that the cost of the purification process of the dehydrogenation product is reduced and the purification device is more energy-saving and environment-friendly.
Fig. 3 shows a flow chart one of a purification process provided in accordance with an exemplary embodiment of the present invention. As shown in fig. 3, the above process may include:
step 301: and sending the gas-phase reaction product and the liquid-phase reaction product generated by the reaction unit into a stripping tower, separating the liquid-phase reaction product by using the stripping tower to obtain a stripped gas-phase product and a stripped liquid-phase product, taking the stripped liquid-phase product as a reaction byproduct, and sending the reaction byproduct out of a purification device to realize the primary separation and purification of the dehydrogenation product.
Step 302: and sending the stripping gas-phase product and the gas-phase reaction product into an absorption tower for absorption and separation to obtain an absorption gas-phase product and an absorption liquid-phase product. The gas phase reaction product generated by the reaction unit is directly sent into the absorption tower communicated with the stripping tower through the top of the stripping tower for absorption and separation, and the liquid phase reaction product generated by the reaction unit is left in the stripping tower for separation, so that the stripping tower only needs to treat the liquid phase reaction product in the reaction product, the treatment capacity of the stripping tower is reduced, the heat or steam amount required in the separation process of the stripping tower is reduced, the cost of the purification process of the exemplary embodiment of the invention is reduced, and the purification process provided by the invention is more energy-saving and environment-friendly.
Step 303: and sending the gas-phase product to a cooling unit for cooling to obtain a gas product and a liquid product. Among the gas products obtained in the cooling unit, the gas product having a volume flow rate of 10% to 30% in the gas at the outlet of the compressor of the first stage or the second stage may be fed into the reaction unit as the reaction gas, and the remaining gas after the multistage compression may be directly output as the gas product. It is to be understood that the volume flow rate herein may be 10%, 20%, 25%, 30%, etc., and is not limited thereto.
As one possible implementation, fig. 4 shows a second flowchart of a purification process provided according to an exemplary embodiment of the present invention. As shown in fig. 4, the above process further includes, before the separation of the liquid phase reaction product by the stripping column:
step 401: and sending the gas-phase reaction product and the liquid-phase reaction product generated by the reaction unit into a product crude separation tank for crude separation to obtain a crude separation gas-phase product and a crude separation liquid-phase product. The gas phase reaction product and the liquid phase reaction product generated by the reaction unit are subjected to coarse separation by using the product coarse separation tank, so that the amount of the liquid phase reaction product sent into the stripping tower is further reduced, the treatment amount of the stripping tower is further reduced, and the purification process provided by the invention is more energy-saving and environment-friendly and has lower cost.
Step 402: and sending the gas-phase product of the crude separation into an absorption tower for separation, and sending the liquid-phase product of the crude separation into a stripping tower for separation.
As one possible implementation, fig. 5 shows a flowchart three of a purification process provided according to an exemplary embodiment of the present invention. As shown in fig. 5, the above process may further include:
step 501: and (3) sending the absorption liquid-phase product into a circulating cooling unit for cooling to obtain a low-temperature liquid-phase product.
Step 502: the low-temperature liquid-phase product is taken as an absorbent to be sent into an absorption tower. The low-temperature liquid phase product is continuously conveyed into the absorption tower through the circulating cooling unit, so that a temperature gradient is formed in the absorption tower, the absorption efficiency is improved, the absorption effect is improved, and the content of heavy components in the finally obtained liquid product is less than 1PPM.
Step 503: and sending the absorption liquid-phase product with the mass flow of 5-25% into a stripping tower for separation so as to remove heavy components in the absorption liquid-phase product, thereby improving the absorption efficiency and the absorption capacity of the absorption liquid-phase product. It is to be understood that the mass flow rate herein may be 5%, 10%, 15%, 20%, 25%, etc., and is not limited thereto.
As one possible implementation, fig. 6 shows a flow chart four of a purification process provided according to an exemplary embodiment of the present invention. As shown in fig. 6, the above process may further include:
Step 601: and pumping the absorption liquid-phase product in the absorption tower by using a circulating pump. For example, the liquid-phase product absorbed in the absorption column can be pumped using a circulation pump and fed into the absorption column to be sprayed as an absorbent.
Step 602: and (3) sending the absorption liquid-phase product pumped by the circulating pump into a cooler for cooling to obtain a low-temperature liquid-phase product. The absorption liquid-phase product pumped by the circulating pump is cooled by using the cooler, so that the low-temperature liquid-phase product sent into the absorption tower can generate temperature difference in the absorption tower and form temperature gradient with the low-temperature liquid-phase product continuously sent into the absorption tower, thereby improving absorption efficiency and absorption capacity, and the content of heavy components in the finally obtained liquid product is less than 1PPM.
Step 603: and sending the absorption liquid-phase product with the mass flow of 5% -25% in the absorption liquid-phase product pumped by the circulating pump into the stripping tower for separation, so as to ensure that the content of heavy components in the absorption liquid-phase product is as low as possible, thereby improving the absorption efficiency and the absorption capacity of the absorption liquid-phase product. It is to be understood that the mass flow rate herein may be 5%, 10%, 15%, 20%, 25%, etc., and is not limited thereto.
As one possible implementation, fig. 7 shows a flowchart five of a purification process provided according to an exemplary embodiment of the present invention. As shown in fig. 7, the above process may further include:
step 701: the absorbed gas phase product is sent into at least one cooling separation component for cooling separation, and a cooling gas product and a cooling liquid product are obtained. The gas product and the liquid product absorbed in the gas phase product can be separated by using the cooling separation assembly.
Step 702: and sending the cooled gas product into a compressor for pressurized separation to obtain a gas product and a pressurized liquid product. It should be understood that the gas product with the volume flow of 10% -30% in the gas at the outlet of the compressor of the first stage or the second stage can be sent into the reaction unit as the reaction gas, and the rest of the gas after the multistage compression is directly output as the gas product. It is to be understood that the volume flow rate herein may be 10%, 20%, 25%, 30%, etc., and is not limited thereto.
Step 703: and outputting the cooling liquid product and the pressurized liquid product with the mass flow rate of 70-100% as liquid products. It is to be understood that the mass flow rate herein may be 70%, 75%, 90%, 97% or 100%, etc., and is not limited thereto.
When at least one cooling separation module is also coupled to the absorber column, the process may further comprise:
step 704: and (3) taking the cooling liquid product with the mass flow of 0-20% as an absorbent to be sent into an absorption tower. It is to be understood that the mass flow rate herein may be 0%, 5%, 10%, 15%, 20%, etc., and is not limited thereto. Because the purity of the cooling liquid product produced in the cooling separation unit is high, when the cooling liquid product with high purity is fed into the absorption tower as an absorbent, a concentration gradient can be formed in the absorption tower, thereby promoting the absorption efficiency and the absorption amount of the absorption tower.
The invention is further illustrated by means of the following examples, which are not intended to limit the scope of the invention. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.
Example 1
This example illustrates the feasibility and energy-saving effect of the dehydrogenation product purification method provided by the invention using cyclohexane-benzene system as an example.
As shown in fig. 1, cyclohexane 101 from outside the boundary region is pressurized by a raw material pump 151, and then mixed with dehydrogenation tail gas 113 (main component is hydrogen and a small amount of benzene) from the compression, and fed into a heat exchanger 152 to be vaporized at a temperature. The vaporized cyclohexane-hydrogen mixture is fed into the reactor 153 after being heated to the reaction temperature (the heating portion may be provided with a heater alone or heating may be effected in the reactor head space). Within reactor 153, one molecule of cyclohexane is stripped of 3 molecules of hydrogen to 1 molecule of benzene, while producing small amounts of heavies such as: biphenyl, and the like. The product (stream 102, which contains benzene, hydrogen and heavy components) after the reaction is cooled in heat exchanger 152 (stream 103) is sent to stripping column 154 where the gas-liquid separation is completed at the top of stripping column 154. The separated liquid phase reaction product and a material flow 108 (the main components comprise benzene and a small amount of heavy components) enter a stripping section tower plate, liquid at the bottom of the stripping tower 154 is heated and gasified by a reboiler 155 and then is sent into the stripping tower for re-separation, and finally heavy components (material flow 115) such as biphenyl and the like are extracted at the bottom of the stripping tower 154 and output as byproducts. The gas phase reaction product 104 separated by the material flow 103 and the gas at the top of the stripping tower 154 are mixed and leave the stripping tower 154 to enter the bottom of the absorption tower 156. The liquid at the bottom of the absorption column 156 (stream 107, which contains benzene and a small amount of heavy components as main components) is fed to the top of the stripping column 154 (stream 108) in a small amount to separate the heavy components therein, and most of the liquid as absorption liquid (stream 109) is circulated to the upper middle portion of the absorption column 156 through a circulation pump 159 and a cooler 160. The top gas (stream 105) of absorber 156 enters cooling assembly 157. A substantial amount of benzene condenses to a liquid in cooling assembly 157 and enters knock-out drum 158 (stream 106). The bottom liquid (primarily benzene) of separator 158 enters the top of absorber 156 as an absorption liquid (stream 110) to further reduce the heavy components in the gas at the top of the absorber column, and the majority (stream 111) exits the apparatus as a liquid product and is sent to a product tank farm (this portion of the plant is not shown).
The gas separated in separator 158 is fed to compressor 161 where it is subjected to multi-stage compression cooling separation and then purified to further recover liquid product (benzene) and to increase the hydrogen pressure, and a portion of the benzene separated at compressor 161 (stream 112) may exit the unit as liquid product. A small amount of the compressor 161 outlet gas (stream 113) from the first or second stage of the multi-stage compression exits the compressor 161 as dehydrogenation tail gas to be mixed with the feedstock 101, reenter the reaction system and recycled to the heat exchanger 152. The remaining gas continues to be compressed and eventually the pressurized gas leaving compressor 161 is sent out of the apparatus as a gaseous product (stream 114) having a major component of hydrogen, containing small amounts of benzene, and other impurities. The hydrogen may be passed through a device such as TSA, PSA, etc. to obtain a technical grade hydrogen product. The flow data for this example are shown in Table 1, with Table 1 showing the mass fractions of the individual streams, wherein the volume fraction of hydrogen in stream 114 is 99.1%.
Table 1 logistics data table
By adopting the process flow provided by the embodiment, the recovery rate of benzene can reach more than 97 percent. The biphenyl content in the product is less than 1PPM. The heat required by the stripping tower reaches 66124 kJ/t-benzene, and the energy-saving effect is remarkable.
Example 2
This example illustrates the feasibility and energy-saving effect of the dehydrogenation product purification method provided by the invention using cyclohexane-benzene system as an example.
As shown in fig. 2, cyclohexane 201 from outside the boundary region is pressurized by a raw material pump 151, and then mixed with dehydrogenation tail gas 215 from the first-stage compression, and enters a heat exchanger 152 to be vaporized at a temperature. The vaporized cyclohexane-hydrogen mixture is fed into the reactor 153 after being heated to the reaction temperature (the heating portion may be provided with a heater alone or heating may be effected in the reactor head space). In the reactor 153, 3 molecules of hydrogen are removed from one molecule of methylcyclohexane and converted to 1 molecule of toluene, and at the same time, a small amount of heavy components are produced, such as: 4, 4-dimethyldicyclohexyl and the like. After cooling in heat exchanger 152 (stream 202), the reacted product (stream 203) is sent to product flash drum 162 for flash distillation. The gas-liquid two-phase separation is achieved in the product coarse separation tank 162. The liquid phase at the bottom of the crude product separation tank 162 is sent into the stripping tower 154, the liquid at the bottom of the stripping tower 154 is heated and gasified by the reboiler 155, then sent into the stripping tower for re-separation, and finally heavy components such as 4, 4-dimethyl dicyclohexyl and the like (material flow 205) are produced at the bottom of the stripping tower 154. The vapor phase at the top of the product crude knockout drum 162 (stream 204) is sent to the bottom of absorber 156 for absorption separation. The liquid at the bottom of absorber 156 (stream 209) enters the top of stripping column 154 (stream 206) in small amounts to separate the heavy components therein, and most of it is recycled as absorber liquid (stream 210) to the upper middle portion of absorber 156 via recycle pump 159 and cooler 160. The top gas of absorber 156 (stream 207) enters cooling assembly 157 and a large amount of toluene condenses to a liquid in cooling assembly 157 and enters separator tank 158 (stream 208). The bottom of separator 158 enters the top of absorber 156 in small amounts as absorption liquid (stream 211) and the majority (stream 212) leaves the apparatus as liquid product and is sent to the product tank farm (this portion of the plant is not shown).
The gas separated in separator tank 158 is fed to compressor 161 where it is subjected to multi-stage compression cooling separation, and then purified to further separate condensed liquid product (stream 213) and to increase the gas pressure, and a portion of the liquid product (stream 213) separated at compressor 161 may be fed to the product tank farm as liquid product leaving the plant. A small amount of the gas (stream 215) at the outlet of the compressor 161 of the first stage or the second stage in the multi-stage compression leaves the compressor 161 as dehydrogenation tail gas to be mixed with the raw material 201, and enters the reaction system again to be circulated to the heat exchanger 152. The remaining gas continues to compress and eventually the pressurized gas leaving compressor 161 is sent out of the apparatus as a gas product (stream 214) having a major component of hydrogen and a minor component of toluene and other impurities. The hydrogen may be passed through a device such as TSA, PSA, etc. to obtain a technical grade hydrogen product. The flow data of this example are shown in Table 2, and the mass fractions of the individual flows are shown in Table 2.
Table 2 logistics data table
By adopting the flow provided by the embodiment, the recovery rate of toluene can reach more than 99 percent. The biphenyl content in the product is less than 1PPM. The heat required by the stripping tower reaches 320513 kJ/t-benzene, and the energy-saving effect is remarkable.
Comparative example 1
Fig. 8 is a schematic view showing the structure of a conventional purifying apparatus according to an exemplary embodiment of the present invention. As shown in FIG. 8, the method and apparatus for carrying out the dehydrogenation product purification scheme in this comparative example will be described with reference to the methylcyclohexane-toluene system as an example.
As shown in fig. 8, methylcyclohexane (stream 501) from the outside of the boundary zone was pressurized by the raw material pump 551 of this comparative example, and then mixed with the dehydrogenation tail gas (stream 511) from the first-stage compression, and the mixed gas was sent to the heat exchanger 552 of this comparative example to be vaporized at a temperature. The vaporized cyclohexane-hydrogen mixture was heated to the reaction temperature (the heating portion may be provided with a heater alone or heating may be effected in the reactor head space) and then fed to the reactor 553 of this comparative example. After cooling in the heat exchanger 552 of this comparative example, the reacted product (stream 502) enters the first product separation tank 554 (stream 503) of this comparative example, and is subjected to gas-liquid separation in the first product separation tank 554 of this comparative example. The gas (stream 504) at the top of the first product separator tank 554 of the present comparative example enters the second product separator tank 556 (stream 505) of the present comparative example through the cooler 555 of the present comparative example, after one or more cooling separations, the liquid (stream 507) condensed at the bottom of the second product separator tank 556 of the present comparative example is sent to the first product separator tank 554 of the present comparative example, or may be sent to the rectifying column 557 of the present comparative example for separation, the liquid phase product (stream 508) at the bottom of the first product separator tank 554 of the present comparative example is sent to the rectifying column 557 of the present comparative example for separation of heavy components (stream 510), the liquid at the bottom of the rectifying column 557 of the present comparative example is sent to the rectifying column 557 for re-separation after being heated by the reboiler 558 of the present comparative example, the gas at the top of the rectifying column 557 of the present comparative example is sent to the rectifying column 559 of the present comparative example and the reflux column 560 of the present comparative example, and the liquid at the bottom of the reflux column 560 of the present comparative example is sent to the rectifying column 557 of the present comparative example for re-separation as the toluene product (stream 509).
The gas (stream 506) at the top of the second product separator tank 556 of this comparative example was cooled and separated by the compressor 561 of this comparative example, and a small amount of the gas (stream 511) at the outlet of the compressor 561 of this comparative example, either the first stage or the second stage in the multistage compression, was taken as dehydrogenation tail gas to leave the compressor 561 of this comparative example and mixed with the raw material 501, and was fed into the reaction system again to be circulated to the heat exchanger 552 of this comparative example. The remaining gas continues to compress and the remaining toluene and gaseous products may be separated (stream 512). This portion of toluene may be sent to the apparatus (stream 513) along with a portion of the liquid at the bottom of the overhead reflux drum 560 of this comparative example, or may be returned to the rectifying column 557 of this comparative example for further separation. The flow data of this example are shown in Table 3, and the mass fractions of the individual flows are shown in Table 3.
TABLE 3 Logistics data Table
By adopting the process flow provided by the comparative example, the recovery rate of toluene can reach more than 99 percent. However, the biphenyl content in toluene is higher, about 1ppm, so that the utilization rate of the recovered toluene is lower, and in the process provided by the comparative example, the heat required by the rectifying tower reaches 884861.5 kJ/t-toluene, and the heat consumption is too high, so that the process cost provided by the comparative example is higher and the requirements of energy conservation and environmental protection are not met.
As can be seen from the processes of comparative examples 1, 2 and 1, when the dehydrogenation product is purified by using the purification equipment and the purification process of the present invention, the heat required by the stripping tower is significantly smaller than that of comparative example 1, and the content of heavy components in the finally recovered liquid product is smaller.
In the above description, technical details of patterning, etching, and the like of each layer are not described in detail. Those skilled in the art will appreciate that layers, regions, etc. of the desired shape may be formed by a variety of techniques. In addition, to form the same structure, those skilled in the art can also devise methods that are not exactly the same as those described above. In addition, although the embodiments are described above separately, this does not mean that the measures in the embodiments cannot be used advantageously in combination.
The embodiments of the present invention are described above. However, these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof. Various alternatives and modifications can be made by those skilled in the art without departing from the scope of the invention, and such alternatives and modifications are intended to fall within the scope of the invention.
Claims (10)
1. A purification apparatus for purification of a dehydrogenation product, the apparatus comprising:
a reaction unit for obtaining a gas phase reaction product and a liquid phase reaction product;
the stripping tower is connected with the reaction unit and is used for separating a liquid phase reaction product sent into the stripping tower by the reaction unit to obtain a stripping gas phase product and a stripping liquid phase product, wherein the stripping liquid phase product is a reaction byproduct;
the absorption tower is connected with the stripping tower and is used for carrying out absorption separation on the stripping gas-phase product sent into the absorption tower by the stripping tower and the gas-phase reaction product sent into the absorption tower to obtain an absorption gas-phase product and an absorption liquid-phase product;
and the cooling unit is connected with the absorption tower and is used for cooling the absorption gas-phase product sent into the cooling unit by the absorption tower to obtain a gas product and a liquid product.
2. The purification apparatus according to claim 1, further comprising a product crude separation tank connected to the reaction unit and the stripping column, respectively, for crude separation of the gas phase reaction product and the liquid phase reaction product to obtain a crude separated gas phase product and a crude separated liquid phase product before the stripping column separates the liquid phase reaction product fed into the stripping column from the reaction unit;
The stripping tower is used for separating the crude separation liquid phase product sent into the stripping tower by the product crude separation tank;
the absorption tower is connected with the product crude separation tank and is used for absorbing and separating the crude separation gas-phase product and the stripping gas-phase product which are sent into the absorption tower by the product crude separation tank.
3. The purification apparatus of claim 1, further comprising a recycle cooling unit coupled to the absorber for cooling the absorption liquid phase product;
the circulating cooling unit is connected with the stripping tower and is used for sending the absorption liquid-phase product with the mass flow of 5% -25% into the stripping tower for separation.
4. A purification apparatus according to claim 3, wherein the circulation cooling unit comprises a circulation pump and a cooler;
the circulating pump is connected with the absorption tower and is used for extracting an absorption liquid-phase product in the absorption tower;
the cooler is connected with the circulating pump and is used for cooling the absorption liquid-phase product pumped by the circulating pump and sending the cooled absorption liquid-phase product into the absorption tower as an absorbent;
The circulating pump is also connected with the stripping tower and is used for sending the absorption liquid-phase product with the mass flow of 5% -25% in the absorption liquid-phase product pumped by the circulating pump into the stripping tower for separation.
5. The purification apparatus of claim 1, wherein the cooling unit comprises:
at least one cooling separation assembly connected to the absorber column for cooling separation of the absorption gas phase product fed into the cooling separation assembly by the absorber column to obtain a cooled gas product and a cooled liquid product;
a compressor connected to at least one of said cooling separation modules for pressure separation of said cooled gas product to obtain said gas product and a pressurized liquid product comprising said cooled liquid product and said pressurized liquid product at a mass flow rate of 80% to 100%; and/or the number of the groups of groups,
at least one of the cooling separation assemblies is connected with the absorption tower and is used for sending the cooling liquid product with the mass flow of 0-20% into the absorption tower as an absorbent.
6. A purification process, characterized by being applied to the purification apparatus of any one of claims 1 to 5, comprising:
Sending a gas phase reaction product and a liquid phase reaction product generated by a reaction unit into a stripping tower, and separating the liquid phase reaction product by using the stripping tower to obtain a stripping gas phase product and a stripping liquid phase product, wherein the stripping liquid phase product is a reaction byproduct;
sending the stripping gas-phase product and the gas-phase reaction product into an absorption tower for absorption and separation to obtain an absorption gas-phase product and an absorption liquid-phase product;
and sending the gas-phase product to the cooling unit for cooling to obtain a gas product and a liquid product.
7. The purification process according to claim 6, characterized by being applied to the purification apparatus of claim 2, the process further comprising, before separating the liquid phase reaction product with the stripping column:
sending the gas phase reaction product and the liquid phase reaction product generated by the reaction unit into a product crude separation tank for crude separation to obtain a crude separation gas phase product and a crude separation liquid phase product;
and sending the crude separation gas-phase product into the absorption tower for separation, and sending the crude separation liquid-phase product into the stripping tower for separation.
8. The purification process according to claim 6, applied to the purification apparatus of claim 3, further comprising:
The absorption liquid-phase product is sent into a circulating cooling unit for cooling, so as to obtain a low-temperature liquid-phase product;
feeding the low temperature liquid phase product as an absorbent into the absorber;
and sending the absorption liquid-phase product with the mass flow of 5-25% into the stripping tower for separation.
9. The purification process according to claim 6, which is applied to the purification apparatus of claim 4, further comprising:
pumping an absorption liquid-phase product in the absorption tower by using a circulating pump;
the absorption liquid-phase product pumped by the circulating pump is sent into a cooler for cooling, so as to obtain a low-temperature liquid-phase product;
and sending the absorption liquid-phase product with the mass flow of 5% -25% in the absorption liquid-phase product pumped by the circulating pump into the stripping tower for separation.
10. The purification process according to claim 6, which is applied to the purification apparatus of claim 5, further comprising:
feeding the absorbed gas phase product into at least one cooling separation assembly for cooling separation to obtain a cooled gas product and a cooled liquid product;
sending the cooled gas product into a compressor for pressurized separation to obtain the gas product and a pressurized liquid product;
Outputting the cooled liquid product and the pressurized liquid product with mass flow of 80% -100% as liquid products; and/or the number of the groups of groups,
and (3) sending the cooling liquid product with the mass flow of 0-20% into the absorption tower as an absorbent.
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