CN113061467A - Liquid paraffin separation system and related chlorinated paraffin production process - Google Patents
Liquid paraffin separation system and related chlorinated paraffin production process Download PDFInfo
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- CN113061467A CN113061467A CN202110313408.4A CN202110313408A CN113061467A CN 113061467 A CN113061467 A CN 113061467A CN 202110313408 A CN202110313408 A CN 202110313408A CN 113061467 A CN113061467 A CN 113061467A
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- 238000000926 separation method Methods 0.000 title claims abstract description 76
- 239000012188 paraffin wax Substances 0.000 title claims abstract description 50
- 229940057995 liquid paraffin Drugs 0.000 title claims abstract description 49
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 12
- 238000004821 distillation Methods 0.000 claims abstract description 97
- 239000001993 wax Substances 0.000 claims abstract description 43
- 239000007788 liquid Substances 0.000 claims abstract description 41
- 239000002994 raw material Substances 0.000 claims abstract description 32
- 239000000463 material Substances 0.000 claims description 28
- 238000009833 condensation Methods 0.000 claims description 10
- 230000005494 condensation Effects 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 8
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 239000000047 product Substances 0.000 description 115
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000004886 process control Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
- C10G73/42—Refining of petroleum waxes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a liquid paraffin separation system and a chlorinated paraffin production process, which comprise the following steps: the liquid wax distillation tower is used for carrying out first separation after raw materials enter to obtain a first top product containing C10-C13 components and C14-C17 components and a first bottom product containing C18-C22 components; the overhead product separation distillation tower is used for carrying out secondary separation after the first overhead product enters to obtain a second overhead product containing C10-C13 components and a second bottom product containing C14-C17 components; the tower bottom product separation distillation tower set comprises three tower bottom products, the first tower bottom product is divided into three strands, the first strand enters an intermediate tank or a direct chlorinated paraffin removal device and is used for producing chlorinated paraffin, the second strand enters a third distillation tower for secondary separation, the third strand enters a fourth distillation tower for secondary separation, the third distillation tower and the fourth distillation tower are separated to obtain a third tower top product containing C18-C19 components, the third tower top product contains C20-C22 components and a third tower bottom product, the carbon number of the obtained product is controlled through each distillation separation, and separation of heavy wax and light wax is achieved.
Description
Technical Field
The invention belongs to the technical field of chemical production, and particularly relates to a liquid paraffin separation system and a related chlorinated paraffin production process.
Background
Coal-made oil is also called coal liquefied oil, liquid fuel and chemical raw materials produced by taking coal as raw materials are used, wherein a part of coal-made oil (coal-made paraffin) is an important raw material for producing chlorinated paraffin at present, the coal-made paraffin is much cheaper than the traditional petroleum-grade paraffin, the lower cost is also the main advantage of producing and popularizing the coal-made oil chlorinated paraffin, the foreign exchange expense of imported petroleum-grade paraffin is saved, and the domestic requirement on the chlorinated paraffin is met.
The liquid paraffin synthesized by the F-T process for preparing the oil from the coal contains more complex components, and comprises SC (generally comprising light liquid paraffin of C10-C13), MC (generally comprising medium liquid paraffin of C14-C17) and LC (generally comprising heavy liquid paraffin of C18-C22), wherein the SC, MC, LC and the liquid paraffin of C18-C19 and C20-C22 in the LC in the chlorinated paraffin production process can respectively and correspondingly produce chlorinated paraffins of different grades, wherein a long-chain liquid paraffin raw material and chlorine gas react under certain conditions to obtain a long-chain chlorinated paraffin product, and the long-chain chlorinated paraffin product is more environment-friendly and safer than a short-chain chlorinated paraffin product.
If the chlorinated paraffin product obtained by processing without distinction is lack of market pertinence and reduces the economic benefit, the separation of heavy raw materials is necessary to optimize the chlorinated paraffin intermediate product.
Disclosure of Invention
The invention aims to provide a liquid paraffin separation system and a chlorinated paraffin production process comprising the same, wherein liquid paraffin synthesized by a coal-to-liquids F-T process is separated, and high-purity liquid paraffin is separated according to carbon number and is used as a raw material for producing chlorinated paraffin.
In order to achieve the above object, the present invention first proposes the following first technical solution:
a liquid paraffin separation system comprising:
a liquid wax distillation tower (C-101), wherein the liquid wax distillation tower (C-101) is used for carrying out first separation after the raw materials enter to obtain a first top product and a first bottom product, the first top product mainly comprises SC products with components of C10-C13 and MC products with components of C14-C17, and the first bottom product mainly comprises LC products with components of C18-C22;
an overhead product separation distillation column (C-102), wherein the overhead product separation distillation column (C-102) is used for carrying out secondary separation after the first overhead product enters to obtain a second overhead product and a second bottom product, the second overhead product mainly comprises an SC product with components of C10-C13, and the second bottom product mainly comprises an MC product with components of C14-C17;
the tower bottom product separation distillation tower set comprises an intermediate tank or a chlorinated paraffin device, a third distillation tower (C-103) and a fourth distillation tower (C-104), wherein the first tower bottom product is divided into three parts, the first part enters the intermediate tank or the direct chlorinated paraffin removal device to produce chlorinated paraffin, the second part enters the third distillation tower (C-103) to be subjected to second separation, the third part enters the fourth distillation tower (C-104) to be subjected to second separation, the third distillation tower (C-103) and the fourth distillation tower (C-104) are separated to obtain a third tower top product and a third tower bottom product, the third tower top product mainly comprises a LC product with a component of C18-C19, and the third tower bottom product mainly comprises a LC product with a component of C20-C22.
Furthermore, the first tower top product requires that the component of C18 is more than or equal to less than 0.1%, the first tower bottom product requires that the component of C17 is less than or equal to less than 0.1%, the second tower top product requires that the component of C14 is more than or equal to less than 2%, the second tower bottom product requires that the component of C13 is less than 0.05%, the third tower top product requires that the component of C20 is more than or equal to less than 0.05%, and the third tower bottom product requires that the component of C19 is less than or equal to less than 0.05%.
Further, the liquid wax distillation column (C-101), the overhead product separation distillation column (C-102), the third distillation column (C-103) and the fourth distillation column (C-104) all adopt vacuum packed columns.
Further, the raw material is liquid paraffin synthesized by a coal-to-liquids F-T process.
Further, the raw material is subjected to first heat exchange with a material extracted from a top full condensation section of the top product separation and distillation tower (C-102), second heat exchange with heavy wax of a material at the bottom of the top product separation and distillation tower (C-102), third heat exchange with a material extracted from a top full condensation section of the liquid wax distillation tower (C-101), fourth heat exchange with heavy wax of a material at the bottom of the liquid wax distillation tower (C-101), and finally enters the liquid wax distillation tower (C-101).
Further, the material extracted from the top fully condensing section of the liquid wax distillation tower (C-101) is condensed or cooled to obtain products of C10-C17.
Further, the liquid wax distillation column (C-101) has an internal top temperature of 55-65 ℃, a pressure of 3-4kPa (a), a bottom temperature of 210-.
Further, the internal tower top temperature of the tower top product separation distillation tower (C-102) is 55-65 ℃, the pressure is 3-4kPa (a), the tower bottom temperature is 183-174 ℃, the pressure is 7-8kPa (a), the hot oil inlet temperature of the reboiler is 300-320 ℃, the pressure is 0.7-0.8MPa (g), the hot oil outlet of the reboiler is 230-270 ℃, and the pressure is 0.65-0.75MPa (g).
Further, the internal top temperature of the third distillation column (C-103) and the fourth distillation column (C-104) is 60-70 ℃, the pressure is 3-4kPa (a), the bottom temperature is 238-.
Further, the invention proposes the following second technical solution:
the chlorinated paraffin production process comprises the liquid paraffin separation system, and the first tower bottom product, the second tower top product, the second tower bottom product, the third tower top product and the third tower bottom product are respectively used as raw materials for producing chlorinated paraffin.
The invention has the beneficial effects that: the system separates products at the top and the bottom of the tower through first distillation, controls the components of the products at the top and the bottom of the tower, then respectively performs second separation on the products at the top and the bottom of the tower, and realizes the separation of heavy wax and light wax by controlling the carbon number of the obtained products each time to obtain high-purity liquid paraffin, wherein SC and LC are separated from the liquid paraffin at the top of the tower, the heavy liquid paraffin LC at the bottom of the tower is divided into three strands, one strand directly produces chlorinated paraffin, the other two strands are subjected to secondary separation to realize balance of productivity, the heavy liquid paraffin is divided into three grades, and the heavy liquid paraffin is used as a raw material for producing chlorinated paraffin to be connected with a chlorinated paraffin production line to produce chlorinated paraffin with different grades correspondingly.
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 principles of the invention and not to limit the invention.
FIG. 1 is a schematic diagram of a liquid paraffin separation system according to the present invention;
FIG. 2 is a schematic process flow diagram of a liquid paraffin separation system according to the present invention;
in the figure: the device comprises a liquid wax distillation tower C-101, a tower top product separation distillation tower C-102, a third distillation tower C-103, a fourth distillation tower C-104, a raw material inlet 1, a tower top product outlet 2, a tower bottom product outlet 3, a reboiler inlet 4 and a reboiler outlet 5.
Detailed Description
The present invention will be further described with reference to the accompanying drawings so as to facilitate the understanding of the present invention by those skilled in the art.
All directional indicators (such as up, down, left, right, front, and rear … …) in the embodiments of the present invention are only used to explain the relative positional relationship between the components, the movement, and the like in a specific posture (as shown in the drawings), and if the specific posture is changed, the directional indicator is changed accordingly. Descriptions such as references to "first", "second", etc. are for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature.
As shown in fig. 1-2, a liquid paraffin separation system includes: a liquid wax distillation tower C-101, a tower top product separation distillation tower C-102 and a tower bottom product separation distillation tower set;
the liquid wax distillation tower C-101 is used for carrying out first separation after raw materials enter to obtain a first top product and a first bottom product, wherein the first top product mainly comprises SC products with components of C10-C13 and MC products with components of C14-C17, and the first bottom product mainly comprises LC products with components of C18-C22;
the overhead product separation distillation column C-102 is used for carrying out secondary separation after the first overhead product enters to obtain a second overhead product and a second bottom product, wherein the second overhead product mainly comprises an SC product with components of C10-C13, and the second bottom product mainly comprises an MC product with components of C14-C17;
the bottom product separation distillation column group comprises: the first bottom product is divided into three parts, the first part enters the intermediate tank or a direct paraffin chloride removal device for producing chlorinated paraffin, the second part enters the third distillation tower C-103 for second separation, the third part enters the fourth distillation tower C-104 for second separation, the third distillation tower C-103 and the fourth distillation tower C-104 are separated to obtain a third top product and a third bottom product, the third top product mainly comprises an LC product with a component of C18-C19, and the third bottom product mainly comprises an LC product with a component of C20-C22.
Furthermore, the first tower top product requires that the component of C18 is more than or equal to less than 0.1%, the first tower bottom product requires that the component of C17 is less than or equal to less than 0.1%, the second tower top product requires that the component of C14 is more than or equal to less than 2%, the second tower bottom product requires that the component of C13 is less than 0.05%, the third tower top product requires that the component of C20 is more than or equal to less than 0.05%, and the third tower bottom product requires that the component of C19 is less than or equal to less than 0.05%.
Further, the liquid wax distillation tower C-101, the overhead product separation distillation tower C-102, the third distillation tower C-103 and the fourth distillation tower C-104 adopt vacuum packed towers.
Specifically, in order to adapt to liquid wax raw materials, the heavy wax rectifying tower adopts structured packing as packing in the tower, and the full condensation section in the tower is cooled and refluxed and the gas at the top of the tower is cooled by water; the material conveying adopts a mechanical vacuum pump, the pre-stage pump adopts a screw rod type, the main pump and the intermediate pump adopt roots vacuum pumps, and the main pump and the intermediate pump are controlled in a variable frequency mode; the safety facilities select ground torches, so that the occupied area is reduced.
Further, the raw material is liquid paraffin synthesized by a coal-to-liquids F-T process.
Further, the raw material and the material extracted from the top full condensation section of the top product separation distillation tower C-102 exchange heat for the first time, and exchange heat with the heavy wax of the bottom material of the top product separation distillation tower C-102 for the second time, and exchange heat with the material extracted from the top full condensation section of the liquid wax distillation tower C-101 for the third time, and exchange heat with the heavy wax of the bottom material of the liquid wax distillation tower C-101 for the fourth time, and finally enter the liquid wax distillation tower C-101.
Further, the materials extracted from the top fully condensing section of the liquid wax distillation tower C-101 are condensed or cooled to obtain products of C10-C17.
Further, the liquid wax distillation column C-101 has an internal top temperature of 55-65 ℃, a pressure of 3-4kPa (a), a bottom temperature of 210-.
Further, the internal tower top temperature of the tower top product separation distillation tower C-102 is 55-65 ℃, the pressure is 3-4kPa (a), the tower bottom temperature is 183-174 ℃, the pressure is 7-8kPa (a), the hot oil inlet temperature of the reboiler is 300-320 ℃, the pressure is 0.7-0.8MPa (g), the hot oil outlet of the reboiler is 230-270 ℃, and the pressure is 0.65-0.75MPa (g).
Further, the internal tower top temperature of the third distillation tower C-103 and the fourth distillation tower C-104 is 60-70 ℃, the pressure is 3-4kPa (a), the tower bottom temperature is 238-.
Specifically, the process comprises the following steps: raw material F-T synthetic liquid paraffin enters a liquid wax distillation tower C-101 from a raw material inlet 1, high-temperature boiling hot oil flows in the tower through a reboiler inlet 4, the raw material F-T synthetic liquid paraffin is separated for the first time in the tower, a first tower top product flows out from a tower top product outlet 2 and then enters a tower top product separation distillation tower C-102, a first tower bottom product flows out from a tower bottom product outlet 3 and then is divided into three strands which respectively enter an intermediate tank or a paraffin chloride device, a third distillation tower C-103 and a fourth distillation tower C-104, hot oil flows out from a reboiler outlet 5 after flowing through the tower, the process principles of the tower top product separation distillation tower C-102, the third distillation tower C-103 and the fourth distillation tower C-104 are similar, specifically, the process control parameters are different, and separation of components with different carbon numbers is realized. The process control parameters are shown in the following table:
| raw materials | Name (R) | Temperature (. degree.C.) | Pressure of | |
| C-101 | F-T synthetic liquid paraffin | C-101 (Top)/(bottom) | 60/225 | 3.5/7.5(kPa)(a) |
| Hot oil inlet of reboiler | 310 | 0.75Mpa(g) | ||
| Hot oil outlet of reboiler | 270 | 0.70Mpa(g) | ||
| C-102 | C-101 top material | C-102 (Top)/(bottom) | 60/189 | 3.5/7.5(kPa)(a) |
| Hot oil inlet of reboiler | 310 | 0.75Mpa(g) | ||
| Hot oil outlet of reboiler | 290 | 0.70Mpa(g) | ||
| C-103 | C-101 substrate material | C-103 (Top)/(bottom) | 65/246 | 3.5/7.5(kPa)(a) |
| Hot oil inlet of reboiler | 310 | 0.75Mpa(g) | ||
| Hot oil outlet of reboiler | 290 | 0.70Mpa(g) | ||
| C-104 | C-101 substrate material | C-104 (Top)/(bottom) | 65/246 | 3.5/7.5(kPa)(a) |
| Hot oil inlet of reboiler | 310 | 0.75Mpa(g) | ||
| Hot oil outlet of reboiler | 290 | 0.70Mpa(g) |
Further, the invention proposes the following second technical solution:
the chlorinated paraffin production process comprises the liquid paraffin separation system, and the first tower bottom product, the second tower top product, the second tower bottom product, the third tower top product and the third tower bottom product are respectively used as raw materials for producing chlorinated paraffin.
Further, the material extracted from the top full condensation section of the liquid wax distillation tower C-101 is condensed and cooled to obtain a product C10-C17 which is also used as a raw material for producing chlorinated paraffin.
Specifically, materials in an oil collecting tank at the top of each tower are pressurized by a pump, one path of the materials is used as hot reflux and is conveyed back to a corresponding distillation tower, the second path of the materials is cooled to a corresponding temperature by an air cooler and a water cooler, one part of the materials is used as cold reflux and is pumped back to the top of the tower, the other part of the materials is sent to a corresponding liquid wax tank, and the materials are sent to an intermediate tank of a corresponding product or a direct paraffin chloride removal device by a pump; after each tower top passes through a full condensation section, non-condensable gas is cooled by a tower top gas water cooler, liquid is separated in a corresponding tower top liquid tank, after the gas is condensed again in a vacuum condenser, the gas is discharged to a torch system through a vacuum pump, the liquid is separated in a corresponding tower top liquid tank, the liquid below the bottom of the liquid separation tank is conveyed to a corresponding liquid wax tank through a tower top pump, and then is conveyed to a corresponding intermediate tank of a product or a direct paraffin chloride removal device through a pump; the tower bottom material is pressurized by a tower bottom liquid pump, cooled by a water cooler, sent to a corresponding heavy wax tank, and then sent to a corresponding product intermediate tank or a direct paraffin chloride removal device by a pump.
The principle of the invention is as follows: the system separates products at the top and the bottom of the tower through first distillation, controls the components of the products at the top and the bottom of the tower, then respectively performs second separation on the products at the top and the bottom of the tower, and realizes the separation of heavy wax and light wax by controlling the carbon number of the obtained products each time to obtain high-purity liquid paraffin, wherein SC and LC are separated from the liquid paraffin at the top of the tower, the heavy liquid paraffin LC at the bottom of the tower is divided into three strands, one strand directly produces chlorinated paraffin, the other two strands are subjected to secondary separation to realize balance of productivity, the heavy liquid paraffin is divided into three grades, and the heavy liquid paraffin is used as a raw material for producing chlorinated paraffin to be connected with a chlorinated paraffin production line to produce chlorinated paraffin with different grades correspondingly.
The process obtains a first bottom product containing C18-C22, a product obtained by condensing or cooling a material extracted from a C-101 top full condensation section of a liquid wax distillation tower of C10-C17, a second top product of C10-C13, a second bottom product of C14-C17, a third top product of C18-C19 and a third bottom product of C20-C22, wherein the carbon chain of the product which is more than or equal to C14 reaches 99.9 percent.
The technical scheme and parameters come from a new heavy wax separation project of Hengyang Shengya chemical engineering science and technology Limited, market raw material heaviness is fully considered, the selected raw material comes from heavy liquid paraffin synthesized by a coal-to-liquid oil F-T process, the raw material is further separated, so that a chlorinated paraffin intermediate product is optimized, the carbon chain composition of the raw material is controlled, the carbon chain of the product is more than or equal to C14 and reaches 99.9%, and the chlorinated paraffin produced by the product meets the environment protection and safety direction.
The above examples are intended to illustrate specific embodiments of the present invention, but not to limit the present invention, and the present invention may be modified and modified without departing from the principle of the present invention, and the modified and modified should be construed as the protection scope of the present invention.
Claims (10)
1. A liquid paraffin separation system, comprising:
the liquid wax distillation tower is used for carrying out first separation after raw materials enter to obtain a first top product and a first bottom product, the first top product mainly comprises SC products with components of C10-C13 and MC products with components of C14-C17, and the first bottom product mainly comprises LC products with components of C18-C22;
an overhead product separation distillation tower, wherein the overhead product separation distillation tower is used for carrying out secondary separation after the first overhead product enters to obtain a second overhead product and a second bottom product, the second overhead product mainly comprises an SC product with components of C10-C13, and the second bottom product mainly comprises an MC product with components of C14-C17;
the tower bottom product separation and distillation tower set comprises an intermediate tank or a chlorinated paraffin device, a third distillation tower and a fourth distillation tower, wherein the first tower bottom product is divided into three strands, the first strand enters the intermediate tank or the chlorinated paraffin device directly for producing chlorinated paraffin, the second strand enters the third distillation tower for secondary separation, the third strand enters the fourth distillation tower for secondary separation, the third distillation tower and the fourth distillation tower are separated to obtain a third tower top product and a third tower bottom product, the third tower top product mainly comprises an LC product with a component of C18-C19, and the third tower bottom product mainly comprises an LC product with a component of C20-C22.
2. The liquid paraffin separation system according to claim 1, wherein the first overhead product requires a composition of not less than C18 < 0.1%, the first bottom product requires a composition of not less than C17 < 0.1%, the second overhead product requires a composition of not less than C14 < 2%, the second bottom product requires a composition of not less than C13 < 0.05%, the third overhead product requires a composition of not less than C20 < 0.05%, and the third bottom product requires a composition of not less than C19 < 0.05%.
3. The liquid paraffin separation system according to claim 2, wherein the liquid paraffin distillation column, the overhead product separation distillation column, the third distillation column and the fourth distillation column each employ a vacuum packed column.
4. The liquid paraffin separation system of claim 1, wherein the raw material is liquid paraffin synthesized by a coal-to-liquid fischer-tropsch process.
5. The liquid paraffin separation system according to claim 4, wherein the raw material is subjected to a first heat exchange with the material extracted from the top full condensation section of the top product separation distillation tower, a second heat exchange with the heavy wax of the bottom material of the top product separation distillation tower, a third heat exchange with the material extracted from the top full condensation section of the liquid wax distillation tower, a fourth heat exchange with the heavy wax of the bottom material of the liquid wax distillation tower, and finally fed into the liquid wax distillation tower.
6. The liquid paraffin separation system of claim 5, wherein the material extracted from the top fully condensing section of the liquid paraffin distillation tower is condensed or cooled to obtain a product of C10-C17.
7. The liquid paraffin separation system according to any one of claims 1 to 6, wherein the liquid paraffin distillation column has an internal column top temperature of 55 to 65 ℃, a pressure of 3 to 4kPa (a), a column bottom temperature of 210-.
8. The liquid paraffin separation system according to any one of claims 1 to 6, wherein the internal overhead temperature of the overhead product separation distillation column is 55-65 ℃, the pressure is 3-4kPa (a), the bottom temperature is 183-.
9. The liquid paraffin separation system according to any one of claims 1 to 6, wherein the internal overhead temperature of the third distillation column and the fourth distillation column is 60-70 ℃, the pressure is 3-4kPa (a), the bottom temperature is 238-.
10. A chlorinated paraffin production process comprising the liquid paraffin separation system according to any one of claims 1 to 9, and using the first bottom product, the second top product, the second bottom product, the third top product, and the third bottom product as raw materials for producing chlorinated paraffin, respectively.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB397169A (en) * | 1932-02-13 | 1933-08-14 | Ig Farbenindustrie Ag | Improvements in the separation of paraffin wax or similar waxy substances from oils containing the same |
| CN109126813A (en) * | 2018-09-17 | 2019-01-04 | 龙岩卓越新能源股份有限公司 | Utilize the method for waste animal and plant fat production atoleine |
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