CN218710200U - Device for producing food additive by using low-freezing-point naphthenic base crude oil distillate - Google Patents
Device for producing food additive by using low-freezing-point naphthenic base crude oil distillate Download PDFInfo
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Abstract
The utility model discloses a device for producing food additives by low-freezing point naphthenic base crude oil distillate, which comprises a raw oil buffer tank, an automatic back-flushing filter, a reaction feeding heating furnace, a hydrotreating reactor, a hydrodewaxing reactor, a high-pressure interstage stripping tower, a high-pressure supplement refining reactor, a heterogeneous dewaxing reactor, a precious metal supplement refining reactor, a hot high-pressure separation tank, a hot low-pressure separation tank, a fractionating system heating feeding furnace, a fractionating tower and a first side line stripping tower which are connected in sequence; also includes a second side stripping column and a third side stripping column; the fractionating tower is circularly connected with the second side line stripping tower, and the second side line stripping tower is connected with the third side line stripping tower. The utility model discloses use low-freezing cycloalkyl crude oil to subtract four lines and subtract bottom oil as the raw materials, produce food additive white oil through the hydrogenation unit after the flow optimization.
Description
Technical Field
The utility model relates to a low-freezing point naphthenic base crude oil processing technology field, more specifically the device that relates to a low-freezing point naphthenic base crude oil distillate oil production food additive that says so.
Background
Naphthenic base crude oil is also called asphalt base crude oil, which is a crude oil containing more naphthenic hydrocarbons. The naphthenic base crude oil has high octane number of gasoline, low cetane number of diesel oil, low wax content or almost no wax content in lubricating oil fraction, low freezing point, low viscosity index and more asphalt in residual oil. The naphthenic base crude oil has poor viscosity-temperature property but low freezing point, and can be used for preparing oil products with low pour point requirement and low viscosity-temperature requirement, such as electric appliance oil, refrigerator oil and the like.
Meanwhile, the low-freezing point naphthenic base crude oil has high acid value, the lubricating oil produced by adopting a furfural refining-clay refining process has poor effect, the problems of equipment corrosion, coking and the like exist in the furfural refining process, the indexes of the product such as chromaticity, oxidation stability and the like are difficult to reach the quality standard, and the increasingly improved environmental protection requirements cannot be further met.
Therefore, the problem to be solved by the technical personnel in the field needs to be solved urgently, how to improve the product quality of the naphthenic base oil and simultaneously investigate the feasibility of a subsequent planning device for producing the food-grade white oil.
SUMMERY OF THE UTILITY MODEL
In view of this, the present invention provides a solution to the deficiencies in the prior art. The utility model discloses use low-freezing cycloalkyl crude oil to subtract four lines and subtract bottom oil as the raw materials, produce food additive white oil through the hydrogenation unit after the flow optimization.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a device for producing food additives by using low-freezing-point naphthenic crude oil distillate oil comprises a raw oil buffer tank, an automatic backwashing filter, a reaction feeding heating furnace, a hydrotreating reactor, a hydrodewaxing reactor, a high-pressure interstage stripping tower, a high-pressure supplement refining reactor, an isomerization dewaxing reactor, a precious metal supplement refining reactor, a hot high-pressure separation tank, a hot low-pressure separation tank, a fractionating system heating feeding furnace, a fractionating tower and a first side line stripping tower which are connected in sequence; the system also comprises a second side stripping tower and a third side stripping tower, wherein the fractionating tower is circularly connected with the second side stripping tower, and the second side stripping tower is connected with the third side stripping tower.
Further, the device for producing the food additive by using the low-freezing-point naphthenic crude oil distillate oil also comprises a feeding pump, wherein the feeding pump is arranged between the automatic backwashing filter and the reaction feeding heating furnace.
Furthermore, the device for producing the food additive by using the low-condensation naphthenic base crude oil distillate also comprises a first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger, a high-pressure stripping gas/second-stage mixed hydrogen heat exchanger, a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I, a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger II and a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger III; the high-pressure stripping gas/first-section mixed hydrogen heat exchanger I is arranged between the high-pressure interstage stripping tower and the high-pressure complementary refining reactor, the high-pressure stripping gas/first-section mixed hydrogen heat exchanger II is arranged between the high-pressure complementary refining reactor and the isomerization dewaxing reactor, and the high-pressure stripping gas/first-section mixed hydrogen heat exchanger III is arranged between the isomerization dewaxing reactor and the precious metal complementary refining reactor.
Further, the device for producing the food additive by using the low-condensation naphthenic base crude oil distillate also comprises a cold high-pressure separation tank, a cold low-pressure separation tank, a circulating hydrogen inlet liquid separation tank and a circulating hydrogen compressor; the hot high-pressure separation tank, the cold high-pressure separation tank and the cold low-pressure separation tank are sequentially connected, the hot low-pressure separation tank and the cold low-pressure separation tank are sequentially connected, and the cold high-pressure separation tank, the circulating hydrogen inlet liquid separation tank and the circulating hydrogen compressor are sequentially connected.
Further, the device for producing the food additive by using the low-freezing naphthenic base crude oil distillate also comprises a hot low-temperature-difference air cooler and a hot high-temperature-difference air cooler; the hot low-pressure separation air cooler is arranged between the hot low-pressure separation tank and the cold low-pressure separation tank, and the hot high-pressure separation air cooler is arranged between the hot high-pressure separation tank and the cold high-pressure separation tank.
Further, the device for producing the food additive by using the low-condensation naphthenic base crude oil distillate also comprises a fractionating tower heat exchanger, a first side line stripping tower heat exchanger and a first side line stripping tower air cooler; the fractionating tower is connected with the fractionating tower heat exchanger in a circulating mode, the first side line stripping tower is connected with the first side line stripping tower heat exchanger in a circulating mode, and the first side line stripping tower is connected with the first side line stripping tower air cooler.
Further, the device for producing the food additive by using the low-freezing-point naphthenic base crude oil distillate also comprises a fractionating tower bottom pump; the fractionating tower bottom pump is arranged between the fractionating tower and the fractionating tower heat exchanger.
Further, the device for producing the food additive by using the low-freezing naphthenic base crude oil distillate also comprises a first side line stripper bottom pump and a third side line stripper bottom pump; the third side line stripping tower is connected with the bottom pump of the third side line stripping tower.
Further, the device for producing the food additive by using the low-freezing-point naphthenic base crude oil distillate also comprises a tail oil pump; the tail oil pump is disposed between the fractionation column and the first side stripper heat exchanger.
Known through foretell technical scheme, compare with prior art, the beneficial effect of the utility model is as follows:
1. the main functions of high-pressure hydrogenation treatment are to remove heterocyclic compounds containing sulfur, nitrogen, oxygen and the like and saturated aromatic hydrocarbons in the raw materials and improve the viscosity-temperature performance and oxidation stability of the oil product. The high-pressure hydrogenation treatment adopts non-noble metal catalyst to deeply modify the oil product.
2. The oil generated by the hydrogenation treatment is subjected to high-pressure hydrodewaxing, and macromolecular normal paraffin with a high pour point is selectively removed, so that the pour point of the oil product meets the requirement. The high-pressure hydrodewaxing adopts a non-noble metal catalyst, and improves the low-temperature fluidity of the oil product.
3. The high-pressure hydrogenation is used for supplementing and refining a small amount of saturated olefin and further saturating aromatic hydrocarbon, so that the chromaticity and the oxidation stability of the oil product are improved. The high-pressure hydrogenation complementary refining adopts a noble metal catalyst, so that the oxidation stability of the oil product is improved.
4. Hydroisomerization dewaxing package technology. The reaction part adopts a process of hydroisomerization and complementary refining, a process of series connection of two reactors of hydroisomerization and hydrorefining is arranged, the reaction part adopts a process of hydroisomerization and complementary refining, and a process of series connection of two reactors of hydroisomerization and hydrorefining is arranged. The catalysts have equivalent activity, the isomerization catalyst has the characteristics of strong isomerization activity, high selectivity of target products and the like, and the supplemented refined catalyst has the characteristics of high hydrogenation and dearomatization activity and the like.
5. The product fractionation process is determined according to the separation sequence of the produced oil components, and the aim is to fractionate the reaction produced oil into various oil products which can meet the market requirements so as to obtain the maximum economic benefit, and the process comprises the factors of product separation degree, product recovery rate, energy utilization efficiency of the separation process, process rationality, complexity, flexibility and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a first part of an apparatus for producing a food additive from naphthenic crude oil distillate oil with low freezing point provided by the present invention;
FIG. 2 is a schematic structural diagram of a second part of the apparatus for producing food additives from naphthenic crude oil distillate oil with low freezing point provided by the present invention;
FIG. 3 is a schematic structural diagram of a third part of the apparatus for producing food additives from naphthenic crude oil distillate oil with low freezing point provided by the present invention;
wherein, 1-raw oil buffer tank, 2-automatic back flushing filter, 3-reaction feeding heating furnace, 4-hydrotreating reactor, 5-hydrodewaxing reactor, 6-high pressure interstage stripping tower, 7-high pressure supplement refining reactor, 8-isomerization dewaxing reactor, 9-noble metal supplement refining reactor, 10-hot high pressure separation tank, 11-hot low pressure separation tank, 12-fractionating system heating feeding furnace, 13-fractionating tower, 14-first side stripping tower, 15-second side stripping tower, 16-third side stripping tower, 17-feeding pump, 18-first section hydrogenation product/first section mixed hydrogen oil heat exchanger, 19-high pressure stripping gas/second section mixed hydrogen heat exchanger, 20-high pressure stripping gas/first section mixed hydrogen heat exchanger I, 21-high pressure stripping gas/first section mixed hydrogen heat exchanger II, 22-high pressure stripping gas/first section mixed hydrogen heat exchanger III, 23-cold high pressure knockout drum, 24-cold low pressure knockout drum, 25-recycle hydrogen inlet liquid separation drum, 26-recycle hydrogen compressor, 27-hot low partial gas air cooler, 28-hot high partial gas air cooler, 29-fractionating tower heat exchanger, 30-first side line stripping tower heat exchanger, 31-first side line stripping tower air cooler, 32-fractionating tower bottom pump, 33-first side line stripping tower bottom pump, 34-third side line stripping tower bottom pump and 35-tail oil pump.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary and intended to be used for explaining the present invention, and should not be construed as limiting the present invention.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used 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 one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," and "fixed" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
In the present disclosure, unless expressly stated or limited otherwise, the first feature "on" or "under" the second feature may comprise direct contact between the first and second features, or may comprise contact between the first and second features not directly. Also, the first feature being "on," "above" and "over" the second feature includes the first feature being directly on and obliquely above the second feature, or merely indicating that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature includes the first feature being directly under and obliquely below the second feature, or simply meaning that the first feature is at a lesser elevation than the second feature.
The embodiment of the utility model discloses a device of low freezing point naphthenic base crude oil distillate oil production food additive, including raw oil buffer tank 1, automatic back flush filter 2, reaction feed heating furnace 3, hydrotreating reactor 4, hydrodewaxing reactor 5, high-pressure interstage stripper 6, high-pressure supplementary refining reactor 7, isomerization dewaxing reactor 8, precious metal supplementary refining reactor 9, hot high-pressure knockout drum 10, hot low pressure knockout drum 11, fractionating system heating feed furnace 12, fractionating tower 13 and first side line stripper 14 that connect gradually; a second side stripper 15 and a third side stripper 16 are included, wherein the fractionation column 13 is connected in a loop with the second side stripper 15 and the second side stripper 15 is connected with the third side stripper 16.
In one embodiment, a feed pump 17 is further included, and the feed pump 17 is disposed between the automatic backwashing filter 2 and the reaction feed heating furnace 3.
In one embodiment, the system also comprises a first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger 18, a high-pressure stripping gas/second-stage mixed hydrogen heat exchanger 19, a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I20, a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger II 21 and a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger III 22; the first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger 18 is arranged between the hydrotreating reactor 4 and the hydrodewaxing reactor 5, the high-pressure stripping gas/second-stage mixed hydrogen heat exchanger 19 is arranged between the hydrodewaxing reactor 5 and the high-pressure interstage stripping tower 6, the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I20 is arranged between the high-pressure interstage stripping tower 6 and the high-pressure supplementary refining reactor 7, the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger II 21 is arranged between the high-pressure supplementary refining reactor 7 and the isomerization dewaxing reactor 8, and the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger III 22 is arranged between the isomerization dewaxing reactor 8 and the precious metal supplementary refining reactor 9.
In one embodiment, a cold high-pressure separator tank 23, a cold low-pressure separator tank 24, a recycle hydrogen inlet knockout drum 25, and a recycle hydrogen compressor 26; wherein, the hot high-pressure separation tank 10, the cold high-pressure separation tank 23 and the cold low-pressure separation tank 24 are sequentially connected, the hot low-pressure separation tank 11 and the cold low-pressure separation tank 24 are sequentially connected, and the cold high-pressure separation tank 23, the recycle hydrogen inlet liquid separation tank 25 and the recycle hydrogen compressor 26 are sequentially connected.
In one embodiment, a hot low-temperature-distribution air cooler 27 and a hot high-temperature-distribution air cooler 28 are further included; wherein, hot low-pressure gas air cooler 27 is arranged between hot low-pressure separating tank 11 and cold low-pressure separating tank 24, and hot high-pressure gas air cooler 28 is arranged between hot high-pressure separating tank 10 and cold high-pressure separating tank 23.
In one embodiment, a fractionator heat exchanger 29, a first side stripper heat exchanger 30, and a first side stripper air cooler 31; wherein, the fractionating tower 13 is circularly connected with the fractionating tower heat exchanger 29, the first side line stripping tower 14 is circularly connected with the first side line stripping tower heat exchanger 30, and the first side line stripping tower 14 is connected with the first side line stripping tower air cooler 31.
In one embodiment, a fractionation bottoms pump 32 is also included; a fractionation column bottom pump 32 is disposed between the fractionation column 13 and the fractionation column heat exchanger 29.
In one embodiment, a first side line stripper bottom pump 33 and a third side line stripper bottom pump 34 are also included; wherein, the first side line stripper bottom pump 33 is arranged between the first side line stripper 14 and the first side line stripper air cooler 31, and the third side line stripper bottom pump 34 is connected with the third side line stripper 16.
In one embodiment, a tail oil pump 35 is also included; a tail oil pump 35 is disposed between the fractionation column 13 and the first side stripper column heat exchanger 30.
The embodiment of the utility model also discloses a method for producing food additives by utilizing the device, which comprises five technical processes of high-pressure hydrogenation treatment, high-pressure hydrodewaxing, high-pressure hydrogenation supplement refining, isomerization dewaxing and precious metal supplement refining, and a product fractionation process;
the method specifically comprises the following steps: raw oil enters a raw oil buffer tank 1 from the outside of the device, mechanical impurities larger than 20 microns in the raw oil are removed through an automatic back-flushing filter 2, the filtered raw oil is pumped to a reaction feeding heating furnace 3, is heated and then enters a hydrotreating reactor 4, then sequentially passes through a hydrodewaxing reactor 5, a high-pressure interstage stripping tower 6, a high-pressure supplementary refining reactor 7, an isomerization dewaxing reactor 8, a precious metal supplementary refining reactor 9, a hot high-pressure separation tank 10, a hot low-pressure separation tank 11 and a fractionating system heating feeding furnace 12 to enter a fractionating tower 13, and finally passes through a first side stripping tower 14 or a second side stripping tower 15 and a third side stripping tower 16 to respectively obtain food-grade white oil.
In one embodiment, the five processes of high-pressure hydrotreating, high-pressure hydrodewaxing, high-pressure hydrofinishing, isodewaxing and precious metal hydrofinishing specifically comprise the following steps:
raw oil enters a raw oil buffer tank 1 from the outside of the device, is pumped out by a raw material booster pump, exchanges heat with an atmospheric and vacuum fractionation part, automatically backflushs a filter 2 to remove mechanical impurities larger than 20 mu m in the oil, enters the filtered raw oil buffer tank 1, and pumps the filtered raw oil to a first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger 18 for heat exchange by a feed pump 17; before entering a first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger 18, oil is mixed with hydrogen from a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I20, the mixed material flow exchanges heat with a reaction product from a 5-hydrodewaxing reactor in the first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger 18, then enters a reaction feeding heating furnace 3, and enters a hydrotreating reactor 4 after being heated;
the hydrotreating reactor 4 is provided with 3 catalyst beds and two hydrogen cooling sections, a hydrotreating reaction product is cooled to 355-396 ℃ by cold hydrogen and then enters a hydrodewaxing reactor 5, the low-temperature fluidity of an oil product is improved under the action of a pour point depressing catalyst, the hydrodewaxing reaction product enters a first-section hydrogenation product/first-section mixed hydrogen oil heat exchanger 18 to exchange heat with mixed hydrogen oil, then the temperature is reduced to 250 ℃, the high-pressure interstage stripping tower 6 is entered, the top gas of the high-pressure interstage stripping tower 6 is subjected to heat exchange by a high-pressure stripping gas/second-section mixed hydrogen heat exchanger 19 and a high-pressure stripping gas/first-section mixed hydrogen heat exchanger I20, then is mixed with circulating hydrogen and deoxygenated water to enter a heat high-pressure gas-air cooler 28 to exchange heat, after the temperature is reduced to 40 ℃, the gas enters a cold high-pressure separation tank 23 to carry out three-phase separation of gas, oil and water, the gas phase is sent to a circulating hydrogen desulfurization system, and then enters a circulating hydrogen compressor 26 after desulfurization;
the recycle hydrogen at the outlet of the recycle hydrogen compressor 26 is divided into three paths, wherein the first path exchanges heat with the gas phase of the high-pressure interstage stripping tower 6 in the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I20, then is mixed with the raw oil, and enters a hot high-pressure gas-separation air cooler 28 for heat exchange; the second path is sent to a hydrotreating reactor 4, a hydrodewaxing reactor 5 and a high-pressure supplementary refining reactor 7 to be used as quenching hydrogen, and the material temperature is adjusted; the third path is mixed with hydrogen from a fresh hydrogen compressor, then enters a high-pressure steam stripping gas/two-stage mixed hydrogen heat exchanger 19 for heat exchange, is mixed with the feed of the high-pressure supplementary refining reactor, and then enters a high-pressure supplementary refining reactor 7; the water phase is sulfur-containing sewage, the sulfur-containing sewage is sent to a water phase section of a cold low-pressure separation tank 24, the separated sulfur-containing sewage is sent to a comprehensive utilization device for low-pressure gas and acid water to be treated, an oil phase is sent to an oil phase section of the cold low-pressure separation tank 24, the oil phase separated from a hot low-pressure separation tank 11 is mixed with oil from the cold low-pressure separation tank 24 and then sent to a low-pressure separation oil/pressure reduction tower bottom oil heat exchanger for heat exchange; the oil phase at the bottom of the high-pressure interstage stripping tower 6 is boosted by a second-stage feed pump 17 and enters a high-pressure supplementary refining reactor 7 together with the mixed hydrogen from a high-pressure stripping gas/second-stage mixed hydrogen heat exchanger 19, a reaction product enters a hot high-pressure separation tank 10, the gas phase of the hot high-pressure separation tank 10 is used as stripping at the bottom of the high-pressure interstage stripping tower 6, the liquid phase of the hot high-pressure separation tank 10 enters a hot low-pressure separation tank 11, and the gas phase of the hot low-pressure separation tank 11 enters a cold low-pressure separation tank 24 after being cooled by a hot low-pressure gas air cooler 27.
In another embodiment, raw oil from the outside of the device is filtered by an automatic back-flushing filter 2 to remove particles larger than 25 μm, then exchanges heat with a No. 6 base oil product, enters a raw oil buffer tank 1 after heat exchange, is mixed with hydrogen after the pressure of the raw oil from the raw oil buffer tank 1 is increased by a hydrogenation feed pump 17, sequentially exchanges heat by a supplementary refining reaction effluent/mixed feed heat exchanger and an isomerization dewaxing reaction effluent/thermal mixed feed heat exchanger, then enters a reaction feed heating furnace 3 to be heated to a required temperature, and enters an isomerization dewaxing reactor 8 to carry out hydrodesulfurization, denitrification and isomerization reactions; the effluent of the isomerization dewaxing reactor 8 is cooled by an isomerization dewaxing reaction effluent/heat mixed feed heat exchanger and then enters a high-pressure supplementary refining reactor 7 for supplementary refining reaction(ii) a The reaction effluent from the supplementary refining reactor is subjected to heat exchange by a supplementary refining reaction effluent/mixed feeding heat exchanger and a supplementary refining reaction effluent/low oil separation heat exchanger in sequence, and then is subjected to high-pressure air cooling to 50 ℃ and enters a high-pressure separator; the high-pressure gas firstly enters an inlet liquid separation tank of the desulfurization reactor, part of carried liquid is separated, and then the high-pressure gas enters the desulfurization reactor to remove H 2 The gas phase at the top of the liquid separation tank enters the recycle hydrogen compressor 26 and is subjected to pressure rise and then is divided into two paths, wherein one path is used as cold hydrogen to control the temperature of the reactor, and the other path is used as recycle hydrogen to be mixed with the make-up hydrogen outside the device to form mixed hydrogen; the high-pressure liquid enters a low-pressure separator under the control of the liquid level; the low-fraction gas is taken as fuel gas and sent out of the device to be taken as fuel gas, and the low-fraction gas enters the fractionating tower 13 after the heat exchange of the supplementary refining reaction effluent/low-fraction oil heat exchanger and the heating of a feeding heating furnace of the fractionating tower 13; the make-up hydrogen from the outside of the device is mixed with the circulating hydrogen into mixed hydrogen after being pressurized by the four stages of the new hydrogen compressor.
In one embodiment, the product fractionation process specifically comprises the steps of:
cooling the overhead gas of the fractionating tower 13 by an air cooler, then feeding the cooled overhead gas into a reflux tank at the top of the fractionating tower 13 for oil, water and gas separation, and directly feeding the overhead gas of the fractionating tower 13 to a fractionating tower 13 feeding heating furnace for fuel; the top liquid of the fractionating tower 13 is boosted by a reflux pump at the top of the fractionating tower 13 and then divided into two paths, one path is used as the top reflux of the fractionating tower 13, and the other path is used as unstable naphtha to be sent out of the device; sending the condensed water separated from the water separation bag of the reflux tank at the top of the fractionating tower 13 to an oil-containing sewage main pipe; the low aromatic solvent oil extracted from the side line flows into a first side line stripping tower 14 for stripping, the heat at the bottom of the first side line stripping tower 14 is provided by a tower bottom reboiler, the top gas of the first side line stripping tower 14 returns to a fractionating tower 13, and the stripped low aromatic solvent oil is subjected to pressure boosting by a first side line stripping tower bottom pump 33, then is cooled by a first side line stripping tower air cooler 31 and then is taken as a product out of the device; the bottom oil of the fractionating tower 13 is boosted by a tail oil pump 35 and then sent to a decompression tower feeding heating furnace, and enters the decompression tower for further separation after being heated to the required temperature;
after the pressure of the tower top of the pressure reducing tower is increased by a pump and air-cooled, one part of the extracted liquid is used as reflux of the tower top of the pressure reducing tower, the other part of the extracted liquid is used as a white oil product and is sent out of the device, 4# base oil extracted from the side line automatically flows into a minus line stripping tower for stripping, a drying tower is arranged at the bottom of a second side line tower, the top gas of the minus line stripping tower returns to the pressure reducing tower, the liquid after stripping automatically flows into the drying tower under the control of the liquid level of the side line tower, the top of the drying tower is vacuumized, the extracted noncondensable gas returns to the stripping of the minus line stripping tower, and the insufficient part is supplemented by steam; boosting the pressure of the No. 4 base oil at the bottom of the drying tower by a pump, then cooling by air cooling, and taking the base oil as a product to be discharged out of the device; the No. 6 base oil extracted from the side line flows into a second-line-reducing stripping tower for stripping, the bottom of a third side line tower is provided with a drying tower, the top gas of the second-line-reducing stripping tower returns to a decompression tower, the liquid after stripping automatically flows into the drying tower under the control of the liquid level, the top of the drying tower is vacuumized, the extracted non-condensable gas returns to the second-line-reducing stripping tower for stripping, and the insufficient part is supplemented by steam; 6# base oil at the bottom of the drying tower is subjected to air cooling after being pressurized by a pump and then is taken as a product to be discharged out of the device; the oil at the bottom of the vacuum tower automatically flows into a lower drying tower under the control of liquid level, the top of the drying tower is vacuumized, the extracted non-condensable gas returns to the vacuum tower for stripping, and the insufficient part is supplemented by steam; the bottom liquid of the drying tower is pressurized by a pump, then is heated by a bottom reboiler at the bottom of a first side line stripping tower and a bottom oil/bottom oil reducing heat exchanger of a stripping tower at an isomerization dewaxing section, and then is cooled by air cooling to be taken as a product to be sent out of the device.
Performance testing
1. Selection of raw materials
1. The naphthenic base oil product properties are compared to the hydrotreater feedstock definition index in table 1.
TABLE 1 comparison of naphthenic base oil product properties with hydrogenation unit feedstock limiting indicators
| Analysis item | Hydrogenated product No. 1 | 2# hydrogenation product | Limit value |
| Density, kg/m 3 | ≤910 | ≤900 | 855 (paraffin base) |
| Sulfur content, ppm | ＜5 | ＜40 | ≤15 |
| Nitrogen content, ppm | ＜2 | ＜20 | ≤3 |
| Aromatic hydrocarbon content% | ≤3 | ≤10 | ≤8 |
| Polycyclic aromatic hydrocarbon content,% | ≤1.5 | ≤3 | - |
| Aromatic index PCI | To be measured | To be measured | < 100 (short term 400) |
Note: the data in table 1 are counted according to the severity values; the density limit value is a limit value for the paraffin-based raw material and is not used as a control index.
2. The food grade white oil product standards are compared to the main indicators of naphthenic base oil product properties in tables 2 and 3.
TABLE 2 food grade white oil product Standard
TABLE 3 naphthenic base oil product index
As can be seen from the initial boiling point and viscosity comparison in tables 2 and 3, the product from No. 1 to No. 1 can be used as the raw material of food-grade white oil. The product from 2# reduction to bottom reduction can be used as the raw material of food-grade white oil after further desulfurization, denitrification and dearomatization (see table 1). From the comparison of viscosity and average molecular weight, only the current minus four-line oil meets the requirement of food grade corresponding grade in the standard. If a food grade white oil is produced, it is advisable to adjust the width of the 1# distillate, to increase the average molecular weight of the product at the corresponding viscosity or to consider analyzing the average molecular weight of the corresponding product to see if it is possible to reconcile. The metal content is expected to meet the requirements.
3. The raw material properties are analyzed in table 4.
TABLE 4 analysis of Properties of the raw materials
As can be seen from Table 4, the sulfur and nitrogen contents of feed 1 and feed 2 meet the feed requirements of the 4# hydrogenation unit and can be used in the experiments. But the relative molecular mass of the raw material 2 can not meet the requirement of No. 4 food-grade white oil.
4. Product 1 (second stage) properties are shown in table 5.
TABLE 5 product 1 (second stage) Properties
2. Process flow adjustment
1. Main device part flow:
according to the communication result with the scientific research institutions, the food-grade white oil cannot be heated by a heating furnace in the fractionation stage, otherwise the easy carbide analysis project cannot pass through. But the product still needs to be dried by a drying tower.
Based on the two points, the process flow adjustment content is as follows: the reaction system has the same flow except that the cold low-fraction oil is sent out. The normal furnace and the reduced furnace of the fractionating system are not heated, and the normal side line are closed. The first side line is reduced, and the tower is vacuumized and dried. The oil is divided into two paths after the first bottom reducing pump. One way enters a second decompression tower for vacuum drying, and then is dried and cooled by a second bottom oil reducing stripping tower, and reversely merged into a second line reducing outlet device pipeline sending device through an unqualified oil outlet device gathering part. And the other path is controlled by a branch hand valve and directly goes to a second reduction line for air cooling, and then is discharged out of the device. The flow chart is as follows:
the execution of the above process needs to be modified in advance: and a pipeline from the outlet of the 2# four-reducing/bottom-reducing oil loading pump to a hydrogenation start-up line is added. The flow chart is as follows:
2. storage and transportation system flow:
the No. 2 minus four-line oil is from a product tank, is converged with a hydrogenation start oil pipeline (needing construction and transformation) through a loading pump and a loading line, is sent into a hydrogenation device, and is sent out of a boundary area after reaction, separation and fractionation. Depending on the feedstock, the product enters 411 or 412 storage tanks. The tank cleaning is needed to ensure the product quality. The tank cleaning requirement is as follows: clear residual oil and general scrubbing are required to reach the condition of no clear water, oil bottom, oil sludge and other impurities.
3. Production operation:
(1) The first reaction also has the function of removing monocyclic aromatic hydrocarbon and is in a kinetic control range, namely the higher the temperature of the first reaction is, the more favorable the removal of the monocyclic aromatic hydrocarbon is. It is recommended that the inverse weighted average temperature be controlled at 310 ℃. (2) The low temperature is favorable for the saturation of polycyclic aromatic hydrocarbon, and the double-inverse weighted average temperature is recommended to be controlled at 230 ℃. Meanwhile, the institute is designed to carry out heat accounting of the reaction part: at 60% feed, the once-through inlet temperature was about 270 ℃. The low-pressure heat exchanger in front of the furnace is changed into steam heat exchange so as to relieve the pressure of insufficient load of the reaction furnace. During the experiment, cold low-oil fraction is separately sent out, most of the side lines of the fractionation system are extracted and closed, and the reaction temperature is increased, and light components are increased.
In the description of the present specification, reference to the description of "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" or the like means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples described in this specification can be combined and combined by those skilled in the art.
Although embodiments of the present invention have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the scope of the present invention.
Claims (9)
1. A device for producing food additives by using low-freezing-point naphthenic crude oil distillate oil is characterized by comprising a raw oil buffer tank, an automatic back-flushing filter, a reaction feeding heating furnace, a hydrotreating reactor, a hydrodewaxing reactor, a high-pressure interstage stripping tower, a high-pressure supplementary refining reactor, an isomerization dewaxing reactor, a precious metal supplementary refining reactor, a hot high-pressure separation tank, a hot low-pressure separation tank, a fractionating system heating feeding furnace, a fractionating tower and a first side line stripping tower which are sequentially connected;
also includes a second side stripping column and a third side stripping column; the fractionating tower is circularly connected with the second side line stripping tower, and the second side line stripping tower is connected with the third side line stripping tower.
2. The apparatus for producing food additive from low freezing point naphthenic crude oil distillate oil of claim 1, further comprising a feed pump;
the feeding pump is arranged between the automatic back-washing filter and the reaction feeding heating furnace.
3. The apparatus for producing food additive from low-freezing naphthenic base crude oil distillate, according to claim 1, further comprising a first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger, a high-pressure stripping gas/second-stage mixed hydrogen heat exchanger, a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I, a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger II and a high-pressure stripping gas/first-stage mixed hydrogen heat exchanger III;
the first-stage hydrogenation product/first-stage mixed hydrogen oil heat exchanger is arranged between the hydrotreating reactor and the hydrodewaxing reactor, the high-pressure stripping gas/second-stage mixed hydrogen heat exchanger is arranged between the hydrodewaxing reactor and the high-pressure interstage stripping tower, the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger I is arranged between the high-pressure interstage stripping tower and the high-pressure supplementary refining reactor, the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger II is arranged between the high-pressure supplementary refining reactor and the isomerization dewaxing reactor, and the high-pressure stripping gas/first-stage mixed hydrogen heat exchanger III is arranged between the isomerization dewaxing reactor and the precious metal supplementary refining reactor.
4. The apparatus for producing food additive from naphthenic crude oil distillate oil with low freezing point as claimed in claim 1, further comprising a cold high-pressure knockout drum, a cold low-pressure knockout drum, a recycle hydrogen inlet liquid separation drum and a recycle hydrogen compressor;
the hot high-pressure separation tank, the cold high-pressure separation tank with the cold low-pressure separation tank connects gradually, the hot low-pressure separation tank with the cold low-pressure separation tank connects gradually, the cold high-pressure separation tank the circulating hydrogen entry divides the fluid reservoir with the circulating hydrogen compressor connects gradually.
5. The apparatus for producing food additive from naphthenic crude oil distillate oil with low freezing point as claimed in claim 4, further comprising a hot low-temperature gas air cooler and a hot high-temperature gas air cooler;
the hot low-pressure separation air cooler is arranged between the hot low-pressure separation tank and the cold low-pressure separation tank, and the hot high-pressure separation air cooler is arranged between the hot high-pressure separation tank and the cold high-pressure separation tank.
6. The apparatus for producing a food additive from low freezing naphthenic crude oil distillate as claimed in claim 1, further comprising a fractionator heat exchanger, a first side stripper heat exchanger and a first side stripper air cooler;
the fractionating tower is circularly connected with the fractionating tower heat exchanger, the first side line stripping tower is circularly connected with the first side line stripping tower heat exchanger, and the first side line stripping tower is connected with the first side line stripping tower air cooler.
7. The apparatus for producing food additive from naphthenic crude oil distillate of low freezing point as claimed in claim 6, further comprising a fractionating tower bottom pump;
the fractionating tower bottom pump is arranged between the fractionating tower and the fractionating tower heat exchanger.
8. The apparatus for producing food additive from naphthenic crude oil distillate of low freezing point as claimed in claim 6, further comprising a first side stripper bottom pump and a third side stripper bottom pump;
the first side line stripping tower bottom pump is arranged between the first side line stripping tower and the first side line stripping tower air cooler, and the third side line stripping tower is connected with the third side line stripping tower bottom pump.
9. The apparatus for producing food additive from naphthenic crude oil distillate oil with low freezing point as claimed in claim 6, further comprising a tail oil pump;
the tail oil pump is arranged between the fractionating tower and the first side line stripping tower heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222595582.5U CN218710200U (en) | 2022-09-29 | 2022-09-29 | Device for producing food additive by using low-freezing-point naphthenic base crude oil distillate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222595582.5U CN218710200U (en) | 2022-09-29 | 2022-09-29 | Device for producing food additive by using low-freezing-point naphthenic base crude oil distillate |
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