CN219399538U - Propane pretreatment system - Google Patents
Propane pretreatment system Download PDFInfo
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- CN219399538U CN219399538U CN202320695743.XU CN202320695743U CN219399538U CN 219399538 U CN219399538 U CN 219399538U CN 202320695743 U CN202320695743 U CN 202320695743U CN 219399538 U CN219399538 U CN 219399538U
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Abstract
The utility model provides a propane pretreatment system, which belongs to the field of propane pretreatment systems and comprises a reaction unit and a dry gas separation unit, wherein the dry gas separation unit comprises a reaction liquid separation tank, an absorption tower and a gas-liquid separation member, an outlet of the reaction unit is connected with an inlet of the reaction liquid separation tank, an outlet of the reaction liquid separation tank is connected with an inlet of the absorption tower, a bottom outlet of the absorption tower is connected with an inlet of the reaction liquid separation tank, a top outlet of the absorption tower is connected with an inlet of the gas-liquid separation member, and an outlet of the gas-liquid separation member is connected with an inlet of the reaction liquid separation tank; the product generated by the reaction of the reaction unit contains dry gas, the dry gas is separated for the first time through the reaction liquid separating tank in advance, then is separated for the second time through the connection of the reaction liquid separating tank and the absorption tower, and finally is separated for the third time through the connection of the absorption tower and the gas-liquid separating piece, and the dry gas in the product is separated step by step so that the dry gas is free from liquid.
Description
Technical Field
The utility model relates to the technical field of propane pretreatment systems, in particular to a propane pretreatment system.
Background
In the propane pretreatment system, after raw materials are reacted and separated, liquid is contained in dry gas discharged from the top of an absorption tower, the dry gas usually directly enters a buffer tank for temporary storage and then enters a fuel gas system for combustion, and the liquid is contained in the dry gas discharged from the absorption tower, so that liquid is carried on the tank bottom of the buffer tank frequently, and the workload of manual liquid discharge is high. In addition, as the liquid phase component is a gasoline component, a great potential safety hazard exists in the discharge process, and in the prior art, the liquid phase component is as follows: 201721082145.6A Chinese patent utility model discloses a naphtha aromatization dry gas treatment device, which comprises a heat exchanger, a carbon four tank and a cooler, wherein the carbon four tank and the cooler are communicated with the heat exchanger, the cooler is also communicated with the carbon four tank, low-temperature dry gas from the carbon four tank and gas phase noncondensable gas from a stable tower top reflux tank are subjected to heat exchange in the heat exchanger and then enter the cooler to be subjected to heat exchange and cooling to form condensate, a gas-liquid mixture which is not condensed in the cooler enters the carbon four tank, and a liquid phase part in the carbon four tank is connected with a carbon four delivery pump which is used for pumping out the liquid phase part in the carbon four tank and sending the liquid phase part into a spherical tank.
Disclosure of Invention
In view of this, the present utility model provides a propane pretreatment system that ensures that no liquids are present in the dry gas.
The technical scheme adopted for solving the technical problems is as follows:
the propane pretreatment system comprises a reaction unit and a dry gas separation unit, wherein the dry gas separation unit comprises a reaction liquid separation tank, an absorption tower and a gas-liquid separation piece, an outlet of the reaction unit is connected with an inlet of the reaction liquid separation tank, an outlet of the reaction liquid separation tank is connected with an inlet of the absorption tower, a bottom outlet of the absorption tower is connected with a first circulation inlet of the reaction liquid separation tank for second dry gas circulation separation, a top outlet of the absorption tower is connected with an inlet of the gas-liquid separation piece, and an outlet of the gas-liquid separation piece is connected with a second circulation inlet of the reaction liquid separation tank for third dry gas circulation separation; after the reaction unit generates a product, the reaction liquid separation tank is used for carrying out first dry gas separation, and then the second dry gas circulation separation and the third dry gas circulation separation are carried out, so that the liquid in the dry gas is separated.
Preferably, the dry gas separation unit further comprises a resolving tower, an inlet of the resolving tower is connected with an outlet of the gas-liquid separation tank, and a top outlet of the resolving tower is connected with a third circulation inlet of the reaction liquid separation tank.
Preferably, the gas-liquid separation member is a desulfurizing tower.
Preferably, the gas-liquid separation member is a gas-liquid separation tank.
Preferably, the reaction unit comprises a raw material feeding pipe, a heater and a reactor, wherein the raw material feeding pipe is connected with the heater, the heater is connected with an inlet of the reactor, and an outlet of the reactor is connected with an inlet of the reaction liquid separation tank.
Preferably, the propane pretreatment system further comprises a product separation unit, wherein the product separation unit comprises a stabilizer column and a depropanizer, an inlet of the stabilizer column is connected with a bottom outlet of the analysis column, and a top outlet of the stabilizer column is connected with an inlet of the depropanizer.
Preferably, the bottom outlet of the stabilizer is connected with the top of the absorber.
Preferably, the product separation unit further comprises a stable light hydrocarbon storage tank, and an inlet of the stable light hydrocarbon storage tank is connected with a bottom outlet of the stabilizer.
Preferably, the bottom outlet of the stabilizer is also connected with the top inlet of the absorber, and a valve is arranged on a pipeline connected with the top inlet of the absorber.
Preferably, the product separation unit further comprises a propane tank, the inlet of the propane tank being connected to the outlet of the depropanizer.
Compared with the prior art, the utility model has the beneficial effects that:
in the propane pretreatment system, the product generated by the reaction of the reaction unit contains dry gas, the dry gas is subjected to primary dry gas separation in advance through the reaction liquid separation tank, then is subjected to secondary dry gas circulating separation through the connection of the reaction liquid separation tank and the absorption tower, and finally is subjected to tertiary dry gas circulating separation through the connection of the absorption tower and the gas-liquid separation piece, so that the dry gas in the product is separated step by step, the liquid is not entrained in the dry gas, the liquid is recycled again, the waste is reduced, the yield of the product is improved, the dry gas is changed from a dry gas non-drying state to a dry gas dry state, and other problems can not occur when the dry gas enters a fuel gas system for combustion.
Drawings
Fig. 1 is a flow chart of a propane pretreatment system.
In the figure: the propane pretreatment system 10, the reaction unit 100, the raw material feed pipe 110, the heater 120, the reactor 130, the dry gas separation unit 200, the reaction liquid separation tank 210, the absorption tower 220, the absorption tower middle section pump 221, the cooler 222, the gas-liquid separation member 230, the analysis tower 240, the product separation unit 300, the stabilizer 310, the valve 311, the depropanizer 320, the stabilized light hydrocarbon storage tank 330, and the propane storage tank 340.
Detailed Description
The technical scheme and technical effects of the embodiments of the present utility model are further described in detail below with reference to the accompanying drawings.
Referring to fig. 1, a propane pretreatment system 10 includes a reaction unit 100, a dry gas separation unit 200, wherein the dry gas separation unit 200 includes a reaction liquid separation tank 210, an absorption tower 220, and a gas-liquid separation member 230, an outlet of the reaction unit 100 is connected to an inlet of the reaction liquid separation tank 210, an outlet of the reaction liquid separation tank 210 is connected to an inlet of the absorption tower 220, a bottom outlet of the absorption tower 220 is connected to a first circulation inlet of the reaction liquid separation tank 210 for performing a second dry gas circulation separation, a top outlet of the absorption tower 220 is connected to an inlet of the gas-liquid separation member 230, and an outlet of the gas-liquid separation member 230 is connected to a second circulation inlet of the reaction liquid separation tank 210 for performing a third dry gas circulation separation; after the reaction unit 100 generates the product, the first dry gas separation is performed by the reaction liquid separation tank 210, and then the second and third dry gas circulation separation are performed, so that the liquid in the dry gas is separated.
Compared with the prior art, the utility model has the beneficial effects that:
in the propane pretreatment system 10, the product generated by the reaction in the reaction unit 100 contains dry gas, the dry gas is separated for the first time through the reaction liquid separation tank 210 in advance, then is separated for the second time through the connection between the reaction liquid separation tank 210 and the absorption tower 220, and finally is separated for the third time through the connection between the absorption tower 220 and the gas-liquid separation element 230, so that the dry gas in the product is separated step by step, the liquid is not entrained in the dry gas, the liquid is recycled again, the waste is reduced, the yield of the product is improved, the dry gas is changed from a dry gas non-drying state to a dry gas drying state, and other problems can not occur when the dry gas enters the fuel gas system for combustion.
Specifically, the middle part of the absorption tower 220 is provided with a middle reflux, the middle oil of the absorption tower 220 is pumped and pressurized by a liquid collecting tank of a middle pump 221 of the absorption tower 220, and then is cooled by a cooler 222 and returned to the tower tray at the upper layer of the tower, so that the absorption effect is enhanced, and the residual heat in the absorption process is removed.
Further, the dry gas separation unit 200 further includes a resolving tower 240, an inlet of the resolving tower 240 is connected to an outlet of the gas-liquid separation tank, an outlet of the resolving tower 240 at a top of the resolving tower is connected to a third circulation inlet of the reaction liquid separation tank 210, a product is separated by the reaction liquid separation tank 210, a liquid enters the resolving tower 240 for resolving, and resolved gas in the liquid enters the reaction liquid separation tank 210 from the top of the resolving tower 240 for re-separation.
Further, the gas-liquid separation member 230 is a desulfurizing tower, and the former raw material is 55% propane containing sulfur, so that sulfur-containing substances such as hydrogen sulfide in the raw material need to be removed in advance, but the components of the raw material are changed, and mixed hydrocarbons (liquefied gas containing gasoline components) in the raw material need not enter the desulfurizing tower to perform desulfurization, and the desulfurizing tower is used as the gas-liquid separation member 230 to perform gas-liquid separation so as to remove liquid phase in dry gas, and the raw material directly enters the reactor 130 through the raw material feeding pipe 110 to perform reactions such as cracking, stacking, aromatization, hydrogen transfer, dehydrogenation and the like, so as to produce fractions rich in propane, light hydrocarbons and residual four carbon.
Further, the gas-liquid separation part 230 is a gas-liquid separation tank, and if the raw material composition changes and contains S, the desulfurizing tower is continuously used for desulfurizing, and the dry gas is separated into gas and liquid by the gas-liquid separation tank.
Further, the reaction unit 100 includes a raw material feeding pipe 110, a heater 120, and a reactor 130, wherein the raw material feeding pipe 110 is connected to the heater 120, the heater 120 is connected to an inlet of the reactor 130, and an outlet of the reactor 130 is connected to an inlet of the reaction liquid separation tank 210.
Further, the propane pretreatment system 10 further includes a product separation unit 300, where the product separation unit 300 includes a stabilizer column 310 and a depropanizer column 320, an inlet of the stabilizer column 310 is connected to a bottom outlet of the analyzing column 240, a top outlet of the stabilizer column 310 is connected to an inlet of the depropanizer column 320, the stabilizer column 310 is a floating valve column, 52 layers of trays are provided, a liquid flowing out from a bottom of the analyzing column 240 enters the stabilizer column 310, a liquefied gas fraction rich in propane enters the depropanizer column 320 from a top of the stabilizer column 310, propane is obtained, a stabilized light hydrocarbon exits from a bottom of the stabilizer column 310, a part enters the stabilized light hydrocarbon storage tank 330, and another part is transported to a top of the absorber column 220 to be used as an absorbent.
Further, the bottom outlet of the stabilizer 310 is connected to the top of the absorber 220.
Further, the product separation unit 300 further includes a stable light hydrocarbon storage tank 330, and an inlet of the stable light hydrocarbon storage tank 330 is connected to a bottom outlet of the stabilizer 310.
Further, the bottom outlet of the stabilizer 310 is further connected to the top inlet of the absorber 220, and a valve 311 is disposed on a pipeline connected to the bottom outlet of the stabilizer 310 and the top inlet of the absorber 220.
Further, the product separation unit 300 further comprises a propane tank 340, the inlet of the propane tank 340 being connected to the outlet of the depropanizer 320.
The following is a procedure for use of the present utility model.
Example 1
The raw materials containing mixed hydrocarbon (liquefied gas containing gasoline components) directly enter the heater 120 through the raw material feeding pipe 110 to be heated, then enter the reactor 130 to be subjected to cracking, stacking, aromatization, hydrogen transfer, dehydrogenation and other reactions, products rich in propane, light hydrocarbon and residual carbon four are produced, the products contain dry gas, the dry gas is subjected to primary dry gas separation in advance through the reaction liquid separation tank 210, then subjected to secondary dry gas circulation separation through the connection of the reaction liquid separation tank 210 and the absorption tower 220, finally subjected to tertiary dry gas circulation separation through the connection of the absorption tower 220 and the gas-liquid separation piece 230, the dry gas in the products is subjected to step-by-step separation, so that the dry gas is not entrained with liquid, the products are separated through the reaction liquid separation tank 210, the liquid enters the analysis tower 240, the liquid enters the reaction liquid separation tank 210 from the top of the analysis tower 240 to be subjected to secondary separation, the liquefied liquid enters the stabilization tower 310, the propane rich fraction enters the stabilization tower top 310 from the top of the reaction liquid separation tank, the light hydrocarbon fraction enters the stabilization tower 320 from the top of the stabilization tower to the absorption tower, and the light hydrocarbon fraction enters the stabilization tower 320 from the light hydrocarbon absorption tower top of the stabilization tower part of the stabilization tower 330 to be subjected to the stabilization tower part of the stabilization tower, and the light hydrocarbon is further separated from the light hydrocarbon absorption tower part of the stabilization tower 310.
The foregoing disclosure is illustrative of the preferred embodiments of the present utility model, and is not to be construed as limiting the scope of the utility model, as it is understood by those skilled in the art that all or part of the above-described embodiments may be practiced with equivalents thereof, which fall within the scope of the utility model as defined by the appended claims.
Claims (10)
1. The propane pretreatment system is characterized by comprising a reaction unit and a dry gas separation unit, wherein the dry gas separation unit comprises a reaction liquid separation tank, an absorption tower and a gas-liquid separation piece, an outlet of the reaction unit is connected with an inlet of the reaction liquid separation tank, an outlet of the reaction liquid separation tank is connected with an inlet of the absorption tower, a bottom outlet of the absorption tower is connected with a first circulation inlet of the reaction liquid separation tank for carrying out second dry gas circulation separation, a top outlet of the absorption tower is connected with an inlet of the gas-liquid separation piece, and an outlet of the gas-liquid separation piece is connected with a second circulation inlet of the reaction liquid separation tank for carrying out third dry gas circulation separation; after the reaction unit generates a product, the reaction liquid separation tank is used for carrying out first dry gas separation, and then the second dry gas circulation separation and the third dry gas circulation separation are carried out, so that the liquid in the dry gas is separated.
2. The propane pretreatment system according to claim 1, wherein the dry gas separation unit further comprises a resolving tower, an inlet of the resolving tower is connected to an outlet of the gas-liquid separation member, and a top outlet of the resolving tower is connected to a third circulation inlet of the reaction liquid separation tank.
3. The propane pretreatment system according to claim 1, wherein the gas-liquid separation member is a desulfurizing tower.
4. The propane pretreatment system of claim 1, wherein the gas-liquid separator is a gas-liquid separator tank.
5. The propane pretreatment system according to claim 1, wherein the reaction unit comprises a raw material feed pipe, a heater, and a reactor, the raw material feed pipe is connected to the heater, the heater is connected to an inlet of the reactor, and an outlet of the reactor is connected to an inlet of the reaction liquid separation tank.
6. The propane pretreatment system of claim 2, further comprising a product separation unit comprising a stabilizer column, a depropanizer column, an inlet of the stabilizer column connected to a bottom outlet of the absorber column, a top outlet of the stabilizer column connected to an inlet of the depropanizer column.
7. The propane pretreatment system of claim 6, wherein a bottom outlet of the stabilizer column is connected to a top of the absorber column.
8. The propane pretreatment system of claim 7, wherein the product separation unit further comprises a steady light hydrocarbon storage tank, an inlet of the steady light hydrocarbon storage tank being connected to a bottom outlet of the steady column.
9. The propane pretreatment system according to claim 8, wherein a bottom outlet of the stabilizer is further connected to a top inlet of the absorber, and a valve is provided on a pipe line in which the bottom outlet of the stabilizer is further connected to the top inlet of the absorber.
10. The propane pretreatment system of claim 9, wherein the product separation unit further comprises a propane tank, an inlet of the propane tank being connected to an outlet of the depropanizer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320695743.XU CN219399538U (en) | 2023-03-31 | 2023-03-31 | Propane pretreatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320695743.XU CN219399538U (en) | 2023-03-31 | 2023-03-31 | Propane pretreatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219399538U true CN219399538U (en) | 2023-07-25 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320695743.XU Active CN219399538U (en) | 2023-03-31 | 2023-03-31 | Propane pretreatment system |
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| Country | Link |
|---|---|
| CN (1) | CN219399538U (en) |
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- 2023-03-31 CN CN202320695743.XU patent/CN219399538U/en active Active
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