CN115999315B - Internal heat integration type absorption stabilization process - Google Patents
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- CN115999315B CN115999315B CN202111224821.XA CN202111224821A CN115999315B CN 115999315 B CN115999315 B CN 115999315B CN 202111224821 A CN202111224821 A CN 202111224821A CN 115999315 B CN115999315 B CN 115999315B
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 127
- 238000000034 method Methods 0.000 title claims abstract description 52
- 230000006641 stabilisation Effects 0.000 title claims abstract description 46
- 238000011105 stabilization Methods 0.000 title claims abstract description 46
- 230000010354 integration Effects 0.000 title claims abstract description 19
- 230000009102 absorption Effects 0.000 claims abstract description 124
- 238000003795 desorption Methods 0.000 claims abstract description 73
- 239000003381 stabilizer Substances 0.000 claims abstract description 29
- 239000007791 liquid phase Substances 0.000 claims abstract description 25
- 230000009103 reabsorption Effects 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 230000000087 stabilizing effect Effects 0.000 claims abstract description 9
- 239000000047 product Substances 0.000 claims description 39
- 238000000926 separation method Methods 0.000 claims description 32
- 238000001816 cooling Methods 0.000 claims description 22
- 239000012071 phase Substances 0.000 claims description 11
- 239000006227 byproduct Substances 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 72
- 230000002745 absorbent Effects 0.000 description 8
- 239000002250 absorbent Substances 0.000 description 8
- 239000006096 absorbing agent Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
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Abstract
The invention discloses an internal heat integration type absorption stabilization process, which is used for treating crude gasoline and rich gas from the top of a fractionating tower and comprises the following steps: adopting an absorption and desorption single tower, wherein the upper part of the absorption and desorption single tower is an absorption section, the lower part of the absorption and desorption single tower is a desorption section, the tower top gas of the absorption and desorption single tower enters a reabsorption tower, and the tower bottom liquid enters a stabilizing tower; at least one gas is pumped out from the desorption section, sequentially exchanges heat with the lower half section of the stabilizer, exchanges heat with the liquid phase of the absorption section through the auxiliary cooler, and is pressurized by the compressor to return to the desorption section. The invention fully utilizes the heat released in the absorption process in the absorption and desorption single tower, and reduces the consumption of external cold source required by the absorption tower and external heat source required by the desorption process.
Description
Technical Field
The invention relates to the technical field of absorption stabilization processes, in particular to an internal heat integration type absorption stabilization process.
Background
The absorption stabilizing system mainly carries out process treatment on the crude gasoline and the rich gas from the fractionating system to produce dry gas, liquefied gas and stable gasoline with qualified vapor pressure. The absorption stabilization process comprises a single-tower process and a double-tower process, wherein the single-tower process is carried out in the same tower by absorption and desorption, the absorption rate and the desorption rate are lower, the energy consumption is higher, and the quality of the product is poor; the double-tower process is that absorption and desorption are respectively carried out in two towers, and becomes the dominant process of the prior refinery absorption stabilization process. The typical technological process of the double-tower absorption stabilization system is that compressed rich gas, rich absorption gasoline and desorbed gas are mixed, cooled by a cooler and then are subjected to balanced flash evaporation in a balance tank, the obtained rich gas enters an absorption tower, and C 3 and above light hydrocarbon components in the rich gas are recovered by using crude gasoline; the lean gas at the top of the absorption tower enters a reabsorption tower for further separation, and the gasoline component carried out at the top of the absorption tower is recovered. The absorbent of the reabsorption tower is light diesel oil from a fractionating tower, the top product of the reabsorption tower is dry gas, and the rich absorption oil at the bottom of the reabsorption tower is sent to the fractionating tower; condensed oil from the balance tank is taken as cold feed and directly enters a desorption tower from the top of the tower, desorption gas is separated from the top of the desorption tower, and deethanized gasoline obtained from the bottom of the tower is sent to a stabilizer for separation. The top product of the stabilizing tower is liquefied gas, the bottom product is stabilized gasoline, one part of the stabilized gasoline is taken as a product sending-out system, and the other part of the stabilized gasoline is sent back to the absorption tower after heat exchange and is taken as a supplementary absorbent for recycling. To increase the absorption efficiency of the absorption tower, an intercooler is generally provided in the absorption tower in the system.
However, there are also a number of problems with the dual column absorption stabilization system: the absorption tower needs to utilize cold energy to remove heat released in the absorption process, and the heat is not fully utilized; the absorbent in the absorption process is a light gasoline component, and the operation load of a desorption tower is large; the stabilizer products are liquefied petroleum gas, light gasoline components and heavy gasoline components, and the products are not subjected to finer separation, so that the fine production and separation of the products are not facilitated; the dry gas component is not fully utilized, and the C 3+ component in the dry gas is more, which is not beneficial to the fine production and separation of the product.
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information forms the prior art already known to a person of ordinary skill in the art.
Disclosure of Invention
One of the purposes of the present invention is to provide an internal heat integration type absorption stabilization process, so as to reduce the consumption requirements of the existing system for external cold sources and external heat sources.
Another object of the present invention is to provide an internal heat integration type absorption stabilization process, whereby the operation load of the system can be reduced.
It is still another object of the present invention to provide an internal heat integration type absorption stabilization process, which can improve the fineness of product separation.
To achieve the above object, the present invention provides an internal heat integrated absorption stabilization process for treating naphtha and rich gas from the top of a fractionation column, comprising: adopting an absorption and desorption single tower, wherein the upper part of the absorption and desorption single tower is an absorption section, the lower part of the absorption and desorption single tower is a desorption section, the tower top gas of the absorption and desorption single tower enters a reabsorption tower, and the tower bottom liquid enters a stabilizing tower; at least one gas is pumped out from the desorption section, sequentially exchanges heat with the lower half section of the stabilizer, exchanges heat with the liquid phase of the absorption section through the auxiliary cooler, and is pressurized by the compressor to return to the desorption section.
In the technical scheme, the rich gas is cooled and separated, and the gas phase and the liquid phase after cooling and separation enter the middle part of the absorption and desorption single tower; the crude gasoline enters the top of the absorption and desorption single tower.
In the technical scheme, the cooling separation comprises primary cooling separation and secondary cooling separation, the gas phase of the rich gas after the primary cooling separation is subjected to secondary cooling separation, and the liquid phase enters the middle part of the absorption and desorption single tower; and the gas phase and the liquid phase after the secondary cooling separation enter the middle part of the absorption and desorption single tower.
Further, in the technical scheme, the top product of the reabsorption tower is lean C2 dry gas, and the bottom liquid enters the upper section of the stabilizer tower; the upper section of the stabilizer is provided with a gamma-shaped baffle, the lower section of the stabilizer is provided with a vertical baffle, a lateral line product at the lower section is divided into two paths, one path of lateral line product enters the top of the reabsorption tower, the other path of lateral line product is discharged outside, the bottom product of the stabilizer is divided into two paths, one path of lateral line product enters the top of the absorption desorption single tower to serve as a supplementary absorbent, and the other path of lateral line product is discharged outside.
Further, in the above technical scheme, the top product of the stabilizer is the C2-rich dry gas, the bottom product is the stabilized gasoline, the upper side product is the liquefied gas, and the lower side product is the C8 component.
In the technical scheme, 2-4 gas streams are pumped out, and each gas stream is subjected to heat exchange with the lower half section of the stabilizer, the auxiliary cooler and the liquid phase of the absorption section in sequence, and then is pressurized by a compressor to return to the desorption section.
In the above technical scheme, the extraction position of the extracted 2-4 gas flows, the position of heat exchange with the lower half section of the stabilizer and the position of liquid phase heat exchange with the absorption section correspond to each other in order.
Further, in the above technical scheme, the pressure difference between the return tower and the outlet tower of each gas drawn from the desorption section is controlled to be 10-100 kPa by adjusting the compression ratio of the compressor.
Further, in the above technical scheme, the temperature difference between the liquid phase temperature of the absorption section to be heat-exchanged and the outlet temperature of the auxiliary cooler is controlled to be 10-15 ℃ by adjusting the cooling depth of the auxiliary cooler.
Further, in the above technical scheme, the operation conditions of the reabsorption tower are as follows: the temperature is 40-200 ℃ and the pressure is 0.1-1.5 MPa.
Further, in the above technical scheme, the operating conditions of the stabilizer are: the temperature is 30-250 ℃ and the pressure is 0.1-1.5 MPa.
Further, in the above technical scheme, the operation conditions of the absorption and desorption single tower are as follows: the temperature is 40-200 ℃; the pressure is 0.1-1.5 MPa.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention fully utilizes the heat released in the absorption process in the absorption and desorption single tower, and reduces the consumption of external cold source required by the absorption tower and external heat source required by the desorption process.
2. The absorption and desorption single tower realizes the heat integrated utilization in the absorption and desorption process and reduces the condensation load of rich gas; the stabilizer utilizes the heat in the system, so that the reboiling load of the stabilizer is reduced; the absorption effect of the C 3+ component in the rich gas is improved, the diesel oil is eliminated as an absorbent in the reabsorption process, and the load of a reabsorption tower is reduced.
3. Through the design has the upper segment and is equipped with the gamma baffle, and the lower segment is equipped with the stabilizer of vertical baffle, and the top of the tower product is rich in C2 dry gas, and upper segment side line product is liquefied gas, and lower segment side line product is the C8 component, and the tower bottom product is stable petrol, and rich in C2 dry gas can directly send to the gas separation device and retrieve C2, and the C8 component can directly be as the raw materials of xylene device, realizes the product and separates in an exquisite way.
4. The multi-strand gas is pumped out to exchange heat correspondingly according to the temperature, so that the cascade utilization of heat is realized, and the utilization rate of heat is improved.
5. And the heat of the absorption section of the absorption and desorption single tower is taken out, the absorption effect is optimized, and the content of C 3+ components in the tower top material is effectively reduced, so that the consumption of the absorber of the reabsorption tower is reduced.
The foregoing description is only an overview of the present invention, and it is to be understood that it is intended to provide a more clear understanding of the technical means of the present invention and to enable the technical means to be carried out in accordance with the contents of the specification, while at the same time providing a more complete understanding of the above and other objects, features and advantages of the present invention, and one or more preferred embodiments thereof are set forth below, together with the detailed description given below, along with the accompanying drawings.
Drawings
Fig. 1 is a schematic flow diagram of an internal heat integration type absorption stabilization process according to an embodiment of the present invention.
Fig. 2 is a schematic flow diagram of a conventional absorption stabilization process.
The main reference numerals illustrate:
101-rich gas, 102-crude gasoline, 111-primary cooler, 112-primary separation tank, 113-secondary cooler, 114-secondary separation tank, 120-absorption desorption single tower, 121-absorption section, 1211-condenser I, 1212-condenser II, 122-desorption section, 130-stabilizer, 131-gamma-type baffle, 132-vertical baffle, 133-intermediate reboiler I, 134-intermediate reboiler II, 140-reabsorption tower, 151-auxiliary cooler I, 152-auxiliary cooler II, 161-compressor I, 162-compressor II;
601-rich gas, 602-crude gasoline, 610-absorber, 611-intercooler, 620-desorber, 621-reboiler I, 631-cooler, 632-balance tank, 640-stabilizer, 641-reboiler II, 650-reabsorber, 651-diesel.
Detailed Description
The following detailed description of embodiments of the invention is, therefore, to be taken in conjunction with the accompanying drawings, and it is to be understood that the scope of the invention is not limited to the specific embodiments.
Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations thereof such as "comprises" or "comprising", etc. will be understood to include the stated element or component without excluding other elements or other components.
Spatially relative terms, such as "below," "beneath," "lower," "above," "upper," and the like, may be used herein for ease of description to describe one element's or feature's relationship to another element's or feature's in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the article in use or operation in addition to the orientation depicted in the figures. For example, if the article in the figures is turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" may encompass both a direction of below and a direction of above. The article may have other orientations (rotated 90 degrees or other orientations) and the spatially relative descriptors used herein interpreted accordingly.
The terms "first," "second," and the like herein are used for distinguishing between two different elements or regions and are not intended to limit a particular position or relative relationship. In other words, in some embodiments, the terms "first," "second," etc. may also be interchanged with one another.
As shown in fig. 1, an internal heat integrated absorption stabilization process according to an embodiment of the present invention is used to treat naphtha 102 and rich gas 101 from the top of a fractionation column. The internal heat integration type absorption stabilization process adopts an absorption and desorption single tower 120, wherein the upper part is an absorption section 121, and the lower part is a desorption section 122. The top gas of the absorption and desorption single column 120 enters a reabsorber 140, and the bottom liquid enters a stabilizer 130. Two gases are extracted from the desorption section 122, the first gas is cooled by an auxiliary cooler I151 after reboiling heat is provided for the lower half section of the stabilizer 130 by an intermediate reboiler I133 in sequence, then the liquid phase temperature is reduced by liquid phase heat exchange between the condenser I1211 and the absorption section 121, the heat of the absorption section 121 is taken away, and the heat is pressurized by a compressor I161 to return to the desorption section 122; the second gas is cooled by the auxiliary cooler II152 after the reboiling heat is provided for the lower half section of the stabilizer 130 by the intermediate reboiler II134 in sequence, then the liquid phase temperature is reduced by the liquid phase heat exchange between the condenser II1212 and the absorption section 121, the heat of the absorption section 121 is taken away, and the pressure is returned to the desorption section 122 by the compressor II 162. Further, the extraction positions of the two extracted gases, the position of heat exchange with the lower half of the stabilizer 130, and the position of liquid phase heat exchange with the absorber 121 correspond in order of height. Illustratively, the first stream is withdrawn at a higher level than the second stream, and the intermediate reboiler I133 is at a higher level than the intermediate reboiler II134 in the stabilizer 130, and the condenser I1211 is at a higher level than the condenser II1212 in the absorber section 121. It should be understood that, in fig. 1, two gases are drawn from the desorption section, the invention is not limited thereto, and those skilled in the art may choose to draw at least one gas, preferably 2-4 gases, according to actual needs, so that heat utilization is more sufficient.
Further, in one or more exemplary embodiments of the present invention, the rich gas 101 is first cooled and separated, and both the cooled and separated gas phase and liquid phase enter the middle of the absorption and desorption single tower 120; the naphtha 102 enters the top of the absorption and desorption unit 120. Illustratively, the cooling separation includes a first-stage cooling separation and a second-stage cooling separation, the rich gas 101 is cooled by the first-stage cooler 111 and then enters the first-stage separation tank 112 for separation, the liquid phase after the first-stage separation enters the middle part of the absorption and desorption single tower 120, and the gas phase enters the second-stage cooler 113 for cooling and then enters the second-stage separation tank 114; the gas phase and the liquid phase separated by the secondary cooling enter the middle part of the absorption and desorption single tower 120.
Further, in one or more exemplary embodiments of the invention, the top product of the reabsorption column 140 is lean C2 dry gas and the bottom liquid enters the upper section of the stabilization column 130. Illustratively, the stabilizer 130 has an upper section provided with a Γ -shaped partition 131, a lower section provided with a vertical partition 132, and the lower side product is divided into two paths, one path entering the top of the reabsorption tower 140 and the other path being discharged. Further, in one or more exemplary embodiments of the invention, the overhead product of the stabilizer 130 is a C2-rich dry gas, which can be directly fed to the gas separation device, the bottom product is stabilized gasoline, the upper side product is liquefied gas, and the lower side product is C8 component.
Further, in one or more exemplary embodiments of the present invention, by adjusting the compression ratio of the compressor, the pressure difference between each gas returning column and the gas exiting column withdrawn from the desorption section is controlled to be 10 to 100kPa, ensuring that the gas can be returned to the absorption desorption single column. Further, in one or more exemplary embodiments of the present invention, a temperature difference between the liquid phase temperature of the absorption stage to be heat-exchanged and the outlet temperature of the auxiliary cooler is controlled to be 10 to 15 ℃ by adjusting the cooling depth of the auxiliary cooler.
Further, in one or more exemplary embodiments of the invention, the operating conditions of the reabsorption column 140 are: the temperature is 40-200 ℃, preferably 40-100 ℃, and the pressure is 0.1-1.5 MPa, preferably 0.1-1.2 MPa.
Further, in one or more exemplary embodiments of the invention, the operating conditions of the stabilization tower 130 are: the temperature is 30 to 250 ℃, preferably 40 to 190 ℃, and the pressure is 0.1 to 1.5MPa, preferably 0.1 to 1.2MPa.
Further, in one or more exemplary embodiments of the invention, the operating conditions of the absorption/desorption single column 120 are: the temperature is 40-200 ℃, preferably 40-150 ℃; the pressure is 0.1 to 1.5MPa, preferably 0.1 to 1.2MPa.
The present invention will be described in more detail by way of specific examples, and it should be understood that the present invention is not limited thereto.
Example 1
Taking an absorption stabilization system of a 180 ten thousand tons/year FCC catalytic cracker as an example, the present embodiment adopts an internal heat integration type absorption stabilization process shown in fig. 1, and part of the bottom liquid of the absorption and desorption single tower and the bottom liquid of the stabilization tower are returned to the tower through reboiling, which is not shown in the figure. The operating conditions in the internal heat integration type absorption stabilization process flow of this example are shown in table 1.
TABLE 1 example 1 internal Heat Integrated absorption stabilization Process flow operating conditions
Comparative example 1
Taking an absorption stabilization system of 180 ten thousand tons per year of FCC catalytic cracker in China as an example, the comparative example adopts the absorption stabilization process shown in FIG. 2 to produce dry gas, liquefied gas and stabilized gasoline. The operating conditions in this comparative absorption stabilization process are shown in table 2.
Table 2 comparative example 1 absorption stabilization process flow operating conditions
The absorption stabilization process comprises: the rich gas 601 is mixed with the absorbed oil from the bottom of the absorption tower 610 and the desorption gas from the top of the desorption tower 620, cooled by a cooler 631, then enters a balance tank 632, the separated gas phase enters the bottom of the absorption tower 610, contacts with the crude gasoline 602 at the top of the tower and the supplemental absorbent at the bottom of the stabilizer 640 in a countercurrent manner, the gas at the top of the absorption tower 610 directly enters the bottom of the reabsorption tower 650, contacts with diesel 651 in a countercurrent manner, further absorbs heavy components carried in the gas phase, and the bottom product of the reabsorption tower 650 is rich absorbed oil and returns to a fractionating tower (not shown in the figure), and the top of the tower is incorporated into a gas pipe network. The liquid phase separated by the balance tank 632 enters the top of the desorption tower 620, a part of the bottom liquid of the desorption tower 620 is reboiled by the reboiler I621 and then returns to the desorption tower 620, and the other part enters the stabilizer 640. The product at the top of the stabilizer 640 is liquefied gas, one part of the bottom liquid of the tower returns to the stabilizer 640 through a reboiler II 641, the other part is divided into two paths, one path is used as a product stabilized gasoline discharging device, and the other path is used as a supplementary absorbent to enter the top of the absorber 610. The absorption column 610 is provided with an intercooler 611.
Compared with comparative example 1, the absorption tower in the technical scheme 1 (figure 1) of the invention has the advantages that the supplementary absorbent of the absorption tower is reduced by 11.6%, the C 3+ content (V%) in the dry gas of the absorption tower is reduced by 10.4%, the flow rate of the C8 component of the stabilizing tower is 12t/h, the reboiling load is reduced by 17.2%, the comprehensive load is reduced by 22.8% (the rich gas cooling load occupies smaller space in the comprehensive load and is not considered), the heat released in the absorption process is fully recycled, the consumption of an external cold source required in the absorption process and an external heat source required in the desorption process is reduced, the C 3+ content in the dry gas is reduced, and the product separation scheme is determined to be C2-rich dry gas by designing a dividing wall rectifying tower type stabilizing tower with an upper-shaped partition board and a lower-shaped vertical partition board, the upper-shaped side line product is liquefied gas, the lower-shaped side line product is C8 component, and the bottom product is stabilized gasoline, so that the product refined separation is realized.
The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. Any simple modifications, equivalent variations and modifications of the above-described exemplary embodiments should fall within the scope of the present invention.
Claims (12)
1. An internal heat integrated absorption stabilization process for treating naphtha and rich gas from the top of a fractionation column comprising:
Adopting an absorption and desorption single tower, wherein the upper part of the absorption and desorption single tower is an absorption section, the lower part of the absorption and desorption single tower is a desorption section, the tower top gas of the absorption and desorption single tower enters a reabsorption tower, and the tower bottom liquid enters a stabilizing tower;
At least one gas is pumped out from the desorption section, sequentially exchanges heat with the lower half section of the stabilizer, exchanges heat with the liquid phase of the absorption section through the auxiliary cooler, and is pressurized by the compressor to return to the desorption section.
2. The internal heat integration type absorption stabilization process according to claim 1, wherein the rich gas is cooled and separated, and the cooled and separated gas phase and liquid phase enter the middle part of the absorption and desorption single tower; the crude gasoline enters the top of the absorption and desorption single tower.
3. The internal heat integration type absorption stabilization process according to claim 2, wherein the cooling separation comprises a first-stage cooling separation and a second-stage cooling separation, the gas phase of the rich gas after the first-stage cooling separation is subjected to the second-stage cooling separation, and the liquid phase enters the middle part of the absorption and desorption single tower; and the gas phase and the liquid phase after the secondary cooling separation enter the middle part of the absorption and desorption single tower.
4. The internal heat integrated absorption stabilization process according to claim 1, wherein the top product of the reabsorption column is lean C2 dry gas and the bottom liquid enters the upper section of the stabilization column; the upper section of the stabilizing tower is provided with a gamma-shaped baffle, the lower section of the stabilizing tower is provided with a vertical baffle, a lateral line product at the lower section is divided into two paths, one path enters the tower top of the reabsorber, and the other path is discharged.
5. The internal heat integration type absorption stabilization process according to claim 4, wherein the top product of the stabilization tower is a C2-rich dry gas, the bottom product is a stabilized gasoline, the upper side product is a liquefied gas, and the lower side product is a C8 component.
6. The internal heat integration type absorption stabilization process according to claim 1, wherein the amount of the extracted gas is 2 to 4, and each gas is sequentially heat-exchanged with the lower half section of the stabilization tower, the auxiliary cooler, and the liquid phase of the absorption section, and then is pressurized by the compressor to return to the desorption section.
7. The internal heat integration type absorption stabilization process according to claim 6, wherein the extraction position of 2 to 4 gas streams extracted, the position of heat exchange with the lower half section of the stabilization tower, and the position of liquid phase heat exchange with the absorption section correspond in order of height.
8. The internal heat integration type absorption stabilization process according to any one of claims 1 to 7, wherein a pressure difference between each gas returning column and each gas exiting column withdrawn from the desorption stage is controlled to be 10 to 100kPa by adjusting a compression ratio of the compressor.
9. The internal heat integration type absorption stabilization process according to any one of claims 1 to 7, wherein the temperature difference between the liquid phase temperature of the absorption stage to be heat exchanged and the outlet temperature of the auxiliary cooler is controlled to be 10 to 15 ℃ by adjusting the cooling depth of the auxiliary cooler.
10. The internal heat integrated absorption stabilization process according to any one of claims 1 to 7, wherein the operating conditions of the reabsorption column are: the temperature is 40-200 ℃ and the pressure is 0.1-1.5 MPa.
11. The internal heat integrated absorption stabilization process according to any one of claims 1 to 7, wherein the operating conditions of the stabilization tower are: the temperature is 30-250 ℃ and the pressure is 0.1-1.5 MPa.
12. The internal heat integration type absorption stabilization process according to any one of claims 1 to 7, wherein the operation conditions of the absorption desorption single tower are: the temperature is 40-200 ℃; the pressure is 0.1-1.5 MPa.
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| CN103865578A (en) * | 2014-02-25 | 2014-06-18 | 中山大学 | Absorption stabilizing device with side draw function and treatment method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103254931A (en) * | 2013-04-12 | 2013-08-21 | 华南理工大学 | Absorption and stabilization system and method for realizing pressure reduction of desorber |
| CN103865578A (en) * | 2014-02-25 | 2014-06-18 | 中山大学 | Absorption stabilizing device with side draw function and treatment method |
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