CN218653721U - Butyl octanol raw materials for production purifier - Google Patents
Butyl octanol raw materials for production purifier Download PDFInfo
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- CN218653721U CN218653721U CN202223200038.2U CN202223200038U CN218653721U CN 218653721 U CN218653721 U CN 218653721U CN 202223200038 U CN202223200038 U CN 202223200038U CN 218653721 U CN218653721 U CN 218653721U
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Abstract
The utility model provides a can adsorb and reduce heat energy loss's butyl octanol raw materials for production purifier to the effective conversion of impurity in the butyl octanol raw materials for production. This butyl octanol raw materials for production purifier includes first heat exchanger, first synthetic gas purifying column, second heat exchanger, synthetic gas heater, second synthetic gas purifying column, third heat exchanger, first propylene purifying column and second propylene purifying column. The utility model discloses a accomplish the conversion and the absorption of impurity in propylene, the synthetic gas under different temperatures to make propylene, the synthetic gas as butyl octanol raw materials for production obtain purifying, the device carries out the coupling with propylene purifying process and synthetic gas purifying process, carries out the step utilization with the heat in the purifying process, makes the heat in the synthetic gas purification be applied to propylene and purifies, improves heat utilization rate, and the device carries out the desorption of layering to impurity, improves the impurity clearance.
Description
Technical Field
The utility model relates to a purifier, concretely relates to butyl octanol raw materials for production purifier belongs to chemical plant technical field.
Background
The production of butanol and octanol usually uses propylene and synthesis gas as raw materials, acetylacetone triphenylphosphine carbonyl rhodium as a catalyst, and triphenylphosphine as a ligand. Among them, propylene and synthesis gas contain impurities such as sulfur, chlorine, and carbonyl iron, which are poisons for rhodium catalysts, and even a small amount of sulfur, chlorine, and carbonyl iron poisons the rhodium catalysts, thereby lowering the production rate of butanol and octanol, and even failing to maintain the production in severe cases. Therefore, the purification of the raw materials for producing the butanol and the octanol is an important link for improving the production rate of the butanol and the octanol, but the purification device for the raw materials for producing the butanol and the octanol in the prior art has single purification flow, and the purification of the propylene and the purification of the synthesis gas are respectively carried out through respective devices, so that the energy consumption is higher.
The Chinese utility model patent with the application number of 2021230232037 discloses a propylene recovery device of a propylene purification system, which comprises a propylene purifier, a propane vaporizer, a propylene recovery tank, a first nitrogen inlet pipeline and a torch system; the propane outlet of the propane vaporizer is connected with the top of the propylene purifier through a pipeline, the bottom of the propylene purifier is connected with the propylene inlet of the propylene recovery tank through a pipeline, the first nitrogen inlet pipeline is connected with the bottom of the propylene purifier, and the top of the propylene purifier is connected with the flare system through a pipeline. This propylene recovery unit retrieves the liquid phase propylene in the propylene clarifier through gasification propane, has effectively reduced the waste and the carbon emission of material, has reduced manufacturing cost, more does benefit to the energy saving and emission reduction of enterprise. However, the apparatus employed by this apparatus has the following drawbacks: the equipment and the process are complex, the operation is not convenient enough, the purification process is still single, the heat energy cannot be effectively utilized, and the purification effect needs to be improved.
SUMMERY OF THE UTILITY MODEL
Based on above background, the utility model aims to provide a can adsorb and reduce heat energy loss's butanol octanol raw materials for production purifier to the effective conversion of impurity in the butanol octanol raw materials for production, solve the background art in the problem.
In order to realize the purpose of the utility model, the utility model provides a following technical scheme:
the utility model provides a butyl octanol raw materials for production purifier, this butyl octanol raw materials for production purifier includes:
the butanol-octanol production raw material purification device comprises a first heat exchanger, a second heat exchanger and a third heat exchanger, wherein the first heat exchanger is provided with a synthesis gas feeding pipeline, the first heat exchanger is communicated with the synthesis gas feeding pipeline, the first heat exchanger also comprises an oxygen injection pipeline, and the synthesis gas feeding pipeline is communicated with the oxygen injection pipeline through a pipeline;
a first syngas purification column in communication with the first heat exchanger via a conduit;
a second heat exchanger in conduit communication with the first heat exchanger, the second heat exchanger in conduit communication with the first syngas purification column;
a syngas heater in communication with the second heat exchanger via a conduit;
a second syngas purification column in conduit communication with a second heat exchanger, the second syngas purification column in conduit communication with a syngas heater;
the device for purifying the butanol and octanol production raw material comprises a first heat exchanger, a second heat exchanger and a third heat exchanger, wherein the first heat exchanger is provided with a propylene feeding line, the third heat exchanger is communicated with the propylene feeding line, the butanol and octanol production raw material purifying device further comprises a water injection pipeline, the propylene feeding line is communicated with a water injection pipeline, and the third heat exchanger is communicated with the first heat exchanger through a pipeline;
the first propylene purification tower is communicated with the outlet of the third heat exchanger through a pipeline;
and the outlet of the second propylene purification tower is communicated with the outlet of the first propylene purification tower through a pipeline.
Preferably, one end of the synthesis gas feeding pipeline is communicated with the first heat exchanger, the other end of the synthesis gas feeding pipeline is provided with a synthesis gas storage tank, and the synthesis gas storage tank is communicated with the synthesis gas feeding pipeline.
Preferably, one end of the oxygen injection pipeline is communicated with a synthesis gas feeding pipeline, the other end of the oxygen injection pipeline is provided with an oxygen storage tank, and the oxygen storage tank is communicated with the oxygen injection pipeline.
Preferably, one end of the propylene feeding line is communicated with the third heat exchanger pipeline, the other end of the propylene feeding line is provided with a propylene storage tank, and the propylene storage tank is communicated with the propylene feeding line.
Preferably, one end of the water injection pipeline is communicated with the propylene feeding line, the other end of the water injection pipeline is provided with a water storage tank, and the water storage tank is communicated with the water injection pipeline.
Preferably, a first adsorption unit is arranged in the first propylene purification tower, the first adsorption unit comprises a plurality of adsorption layers, and the adsorption layers are fixedly connected with the first propylene purification tower.
Preferably, a second adsorption unit is arranged in the second propylene purification tower, and the second adsorption unit is fixedly connected with the second propylene purification tower.
Preferably, the first syngas purification tower is a vertical packed bed tower, a third adsorption unit is arranged in the first syngas purification tower, and the third adsorption unit is fixedly connected with the first syngas purification tower.
Preferably, the second synthesis gas purification tower is a vertical packed bed tower, a plurality of beds are arranged in the second synthesis gas purification tower, a supporting plate is arranged at the bottom of each bed, and a pressing plate is arranged at the top of the uppermost bed.
Preferably, a propylene collector is arranged at the bottom of the second propylene purification tower, and the propylene collector is communicated with the second propylene purification tower through a pipeline.
Compared with the prior art, the utility model has the advantages of it is following:
the utility model discloses a butyl octanol raw materials for production purifier utilizes the different absorption units that each part of device set up, through accomplish propylene under different temperatures, the conversion and the absorption of impurity in the synthetic gas, thereby make as butyl octanol raw materials for production's propylene, the synthetic gas obtains purifying, the device carries out the coupling with propylene purifying process and synthetic gas purifying process, the heat that will purify in-process carries out the step utilization, the heat that makes in the synthetic gas purification is applied to propylene and purifies, improve heat utilization rate, the device carries out the desorption of layering to impurity, improve the impurity clearance.
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.
Figure 1 is the structure schematic diagram of the butanol and octanol production raw material purification device of the utility model.
In the figure: 1. a first heat exchanger; 2. a first syngas purification column; 3. a second heat exchanger; 4. a syngas heater; 5. a second syngas purification column; 6. a third heat exchanger; 7. a first propylene purification column; 8. a second propylene purification tower; 9. a syngas feed line; 10. an oxygen injection line; 11. a propylene feed line; 12. a water injection line.
Detailed Description
The technical solution of the present invention is further specifically described below by way of specific embodiments and with reference to the accompanying drawings. It is to be understood that the practice of the invention is not limited to the following examples, and that any modifications and/or changes in form made to the invention are intended to fall within the scope of the invention.
In the utility model, all parts and percentages are weight units, and the adopted equipment, raw materials and the like can be purchased from the market or commonly used in the field if not specified. The methods in the following examples are conventional in the art unless otherwise specified. The components or devices in the following examples are, unless otherwise specified, standard parts or parts known to those skilled in the art, the structure and principle of which are known to those skilled in the art through technical manuals or through routine experimentation.
In the following detailed description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the embodiments of the invention. However, one or more embodiments may be practiced without these specific details by one of ordinary skill in the art.
A purification apparatus for butanol and octanol production raw material as shown in fig. 1, which comprises a first heat exchanger 1, a first synthesis gas purification tower 2, a second heat exchanger 3, a synthesis gas heater 4, a second synthesis gas purification tower 5, a third heat exchanger 6, a first propylene purification tower 7 and a second propylene purification tower 8.
First heat exchanger 1 the first heat exchanger 1 is in communication with a syngas feed conduit, and the first heat exchanger 1 tube side is connected to the second heat exchanger 3 shell side. The shell side is unpurified synthetic gas, the tube side is purified synthetic gas, and the first heat exchanger 1 is communicated with an oxygen injection pipeline 10 through a pipeline.
First synthetic gas purifying column 2 the first synthetic gas purifying column 2 is a vertical column, an adsorbent is arranged in the first synthetic gas purifying column 2, the top of the first synthetic gas purifying column 2 is connected with the shell side of the first heat exchanger 1, and the bottom of the first synthetic gas purifying column 2 is connected with the tube side of the second heat exchanger 3.
Second heat exchanger 3 the tube side of second heat exchanger 3 is connected with first synthesis gas purification tower 2 and synthesis gas heater 4, and the shell side of second heat exchanger 3 is connected with second synthesis gas purification tower 5 and first heat exchanger 1 tube side synthesis gas heater 4.
The tube pass of the synthesis gas heater 4 is connected with a second synthesis gas purification tower 5.
Second synthetic gas purifying tower 5 the second synthetic gas purifying tower 5 is connected with the shell side of the second heat exchanger 3.
First propylene purifying column 7 the export of 7 bottoms of first propylene purifying column is connected with 8 tops of second propylene purifying column, and 8 bottoms of second propylene purifying column export are the propylene after purifying.
The first heat exchanger 1, the second heat exchanger 3, and the syngas heater 4 are tubular heat exchangers, preferably fixed-tube plate type heat exchangers.
The first synthesis gas purification tower 2, the second synthesis gas purification tower 5, the first propylene purification tower 7 and the second propylene purification tower 8 adopt a horizontal tank body or a vertical tank body, a vertical tank body is adopted in the embodiment, and a distributor is arranged at an inlet, so that impact on a catalyst bed layer is prevented.
The synthesis gas heater 4 is heated by steam, and the grade of the steam meets the purification requirement.
One end of a synthesis gas feeding pipeline 9 is communicated with the first heat exchanger 1, the other end of the synthesis gas feeding pipeline 9 is provided with a synthesis gas storage tank, and the synthesis gas storage tank is communicated with the synthesis gas feeding pipeline 9.
One end of the oxygen injection pipeline 10 is communicated with a synthetic gas feeding pipeline, and the other end of the oxygen injection pipeline 10 is provided with an oxygen storage tank which is communicated with the oxygen injection pipeline 10.
One end of the propylene feeding line 11 is communicated with the third heat exchanger 6 through a pipeline, the other end of the propylene feeding line 11 is provided with a propylene storage tank, and the propylene storage tank is communicated with the propylene feeding line 11.
12 one ends of water injection pipeline and the 11 intercommunications of propylene feed line, 12 other ends of water injection pipeline are provided with the water storage tank, and the water storage tank communicates with 12 water injection pipelines.
Be provided with first adsorption unit in the first propylene purge tower 7, first adsorption unit includes a plurality of adsorbed layers, a plurality of adsorbed layers and first propylene purge tower 7 fixed connection. In this embodiment, three adsorption layers are provided, and alumina, zinc oxide, and copper-impregnated activated carbon are sequentially filled from top to bottom.
The inside second absorption unit that is provided with of second propylene purifying tower 8, second absorption unit and second propylene purifying tower 8 fixed connection. The second adsorption unit is provided with a layer of palladium-based alumina as an adsorbent.
The first synthetic gas purification tower 2 is a vertical packed bed tower, a third adsorption unit is arranged in the first synthetic gas purification tower 2, and the third adsorption unit is fixedly connected with the first synthetic gas purification tower 2.
The second synthetic gas purification tower 5 is a vertical packed bed tower, a plurality of beds are arranged inside the second synthetic gas purification tower 5, a supporting plate is arranged at the bottom of each bed, and a pressing plate is arranged at the top of the uppermost bed.
The bottom of the second propylene purification tower 8 is provided with a propylene collector, and the propylene collector is communicated with the second propylene purification tower 8 through a pipeline.
The following is to take this butyl octanol raw materials for production purifier to be applied to concrete butyl octanol production as an example the utility model discloses a device theory of operation explains in detail.
The components of the raw material propylene and the raw material synthesis gas which are treated by the butanol-octanol production raw material purification device are shown in the table I and the table II.
Table one raw material syngas composition
Propylene component of TABLE II raw Material
The purification process of the synthesis gas comprises the following steps:
the pressure of the synthesis gas is 2.0-3.0 Mpag, the synthesis gas enters the first heat exchanger 1 through a pipeline, and the oxygen content in the synthesis gas is controlled to be 2-5 molppm and is heated to 80-95 ℃ by the synthesis gas from the second heat exchanger 3 at 100-120 ℃. When the outlet temperature of the first heat exchanger 1 is too high, the amount of the bypass entering the first heat exchanger 1 is increased, and the amount of the bypass entering the first heat exchanger 1 is reduced. When the outlet temperature of the first heat exchanger 1 is too low, the amount of the bypass entering the first heat exchanger 1 is reduced, and the amount of the bypass entering the first heat exchanger 1 is increased. The temperature of the synthesis gas is 80-90 DEG CThe mixture enters a first synthesis gas purification tower 2, activated carbon with the diameter of 1.7 to 3.35mm is filled in the tower, and the bulk density is 480 to 520Kg/m 3 Carbonyl iron Fe (CO) 5 And nickel carbonyl Ni (CO) 4 Respectively react with oxygen at the temperature of 80-95 ℃ to generate Fe 2 O 3 NiO and CO, fe 2 O 3 And NiO was adsorbed by activated carbon. The total amount of carbonyl iron and carbonyl sulfur discharged from the bottom of the first synthesis gas purification tower 2 is less than 0.05ppm.
The synthesis gas without the iron carbonyl and the nickel carbonyl enters a tube pass of a second heat exchanger 3, the synthesis gas with the high temperature of 180-190 ℃ from the bottom of a second synthesis gas purification tower 5 enters a shell pass of the second heat exchanger 3, the waste heat of the synthesis gas without the iron carbonyl and the nickel carbonyl is heated to 130-150 ℃, and then the synthesis gas enters a synthesis gas heater 4, and the synthesis gas without the iron carbonyl and the nickel carbonyl is heated to 180-190 ℃ by 2.0Mpag steam in the shell pass of the synthesis gas heater 4.
The top of the second synthesis gas purification tower 5 is provided with platinum-based alumina which is macroporous gamma-Al 2 O 3 The active component Pt is uniformly dispersed on the carrier, the obvious macroporous distribution and the active component uniformly dispersed in the adsorbent are beneficial to accelerating the adsorption rate, reducing a mass transfer area and providing excellent adsorption capacity, the oxygen can be hydrogenated and converted into water, and meanwhile, the organic sulfur and the organic chlorine are converted into inorganic sulfur and inorganic chlorine, and the removal precision of the sulfur and the chlorine is ensured. The particle size of the platinum-based alumina
The bulk density is 0.48-0.58 g/ml, and the specific surface is more than or equal to 200m 2 G, pore volume is more than or equal to 0.60cm 3 The Pt content is 0.09-0.10 wt%. Caustic alumina with the grain diameter phi of 2-3 mm and the bulk density of 0.7-1.0 kg/l is filled in the middle part of the second synthesis gas purification tower 5, and chloride is removed in the bed layer. The bottom of the second synthesis gas purification tower 5 is filled with zinc oxide with the grain diameter phi of 3-4.5 mm, the bulk density of 1.0-1.2 kg/l and H 2 S reacts with zinc oxide to form zinc sulfide, hydrogen cyanide is hydrolyzed to form ammonia and carbon monoxide, and the ammonia is adsorbed by the zinc oxide.
The synthesis gas at the bottom of the second synthesis gas purification tower 5 completes the purification process, and the temperature of the synthesis gas is 180-190 ℃ at this time, so as to heat the synthesis gas entering the second heat exchanger 3 for removing the carbonyl iron and the carbonyl nickel. The temperature of the purified synthesis gas is then reduced to 100-120 c and used as the heat source for the first heat exchanger 1. The composition of the purified synthesis gas is shown in table three.
Table III purified syngas Components
The purification process of the propylene comprises the following steps:
the pressure of the propylene is 2.5-3.0 Mpag, a certain amount of water is injected, the water content in the propylene is controlled to be 5-15 ppm, the propylene enters the shell pass of the third heat exchanger 6 through a pipeline, the synthesis gas from the tube pass of the first synthesis gas heat exchanger enters the tube pass of the third heat exchanger 6, the propylene is heated to 40-50 ℃, and then the propylene enters the first propylene purification tower 7.
The top of the first propylene purifying tower 7 is filled with active alumina with grain diameter phi of 3-5 mm and bulk density of 0.7-0.9 kg/l, wherein COS and CS can be treated 2 Hydrolysis of organic sulfur to H 2 S, the surface of the activated alumina has great chemical adsorption effect and can also adsorb other organic sulfides, chlorides, cyanides and other common poisons.
The middle part of the first propylene purifying tower 7 is filled with zinc oxide, the grain diameter phi is 2-5 mm, the bulk density is 0.4-0.6 kg/l, and hydrogen sulfide and hydrogen chloride which are not removed completely in an active alumina bed layer are further removed.
The bottom of the first propylene purifying tower 7 is filled with copper-impregnated active carbon, the particle diameter is phi 3-5 mm x (5-12) mm, the bulk density is 0.9-1.1 kg/l, and hydrogen sulfide and hydrogen chloride which are not completely removed in an active alumina and zinc oxide bed layer are removed.
The propylene from the bottom of the first propylene purifying tower 7 is added with hydrogen before entering the second propylene purifying tower 8, the concentration of the hydrogen is controlled to be 30-100 ppm, the second propylene purifying tower 8 is filled with palladium-based alumina, the particle size phi is 3-5 mm, the bulk density is 0.7-0.9 kg/l, oxygen can be hydrogenated to generate water, and unsaturated hydrocarbons are hydrogenated to generate saturated hydrocarbons. The propylene composition after purification is shown in Table four.
TABLE IV propylene component after purification
According to the data, the butanol and octanol production raw material purification device is coupled with the purification of synthesis gas through the purification of propylene, the heat in the purification process is utilized to the greatest extent, the impurities are removed in a layered mode, and the removal effect is good.
The principles and embodiments of the present invention have been explained herein using specific examples, and the above descriptions of the embodiments are only used to help understand the method and its core ideas of the present invention. It should be noted that, for those skilled in the art, without departing from the principle of the present invention, the present invention can be further modified and modified, and such modifications and modifications also fall within the protection scope of the appended claims.
Claims (10)
1. The utility model provides a butyl octanol raw materials for production purifier which characterized in that: this butyl octanol raw materials for production purifier includes:
the device for purifying the butanol and octanol production raw materials comprises a first heat exchanger (1), wherein the first heat exchanger (1) is provided with a synthesis gas feeding pipeline (9), the first heat exchanger (1) is communicated with the synthesis gas feeding pipeline (9), the device further comprises an oxygen injection pipeline (10), and the synthesis gas feeding pipeline (9) is communicated with the oxygen injection pipeline (10) through a pipeline;
a first syngas purification column (2), the first syngas purification column (2) being in communication with the first heat exchanger (1) via a conduit;
a second heat exchanger (3), wherein the second heat exchanger (3) is communicated with the first heat exchanger (1) through a pipeline, and the second heat exchanger (3) is communicated with the first synthesis gas purification tower (2) through a pipeline;
the synthesis gas heater (4), the synthesis gas heater (4) is communicated with the second heat exchanger (3) through a pipeline;
the second synthesis gas purification tower (5), the second synthesis gas purification tower (5) is communicated with the second heat exchanger (3) through a pipeline, and the second synthesis gas purification tower (5) is communicated with the synthesis gas heater (4) through a pipeline;
a third heat exchanger (6), wherein the third heat exchanger (6) is provided with a propylene feeding line (11), the third heat exchanger (6) is communicated with the propylene feeding line (11), the butanol and octanol production raw material purification device further comprises a water injection pipeline (12), the propylene feeding line (11) is communicated with a water injection pipeline, and the third heat exchanger (6) is communicated with the first heat exchanger (1) through a pipeline;
the first propylene purification tower (7), the first propylene purification tower (7) is communicated with the outlet of the third heat exchanger (6) through a pipeline;
and the outlet of the second propylene purification tower (8) is communicated with the outlet of the first propylene purification tower (7) through a pipeline.
2. The apparatus for purifying butanol and octanol production raw material according to claim 1, wherein: one end of the synthesis gas feeding pipeline (9) is communicated with the first heat exchanger (1), the other end of the synthesis gas feeding pipeline (9) is provided with a synthesis gas storage tank, and the synthesis gas storage tank is communicated with the synthesis gas feeding pipeline (9).
3. The purification device for butanol and octanol production raw materials as claimed in claim 1, wherein: one end of the oxygen injection pipeline (10) is communicated with a synthetic gas feeding pipeline, the other end of the oxygen injection pipeline (10) is provided with an oxygen storage tank, and the oxygen storage tank is communicated with the oxygen injection pipeline (10).
4. The apparatus for purifying butanol and octanol production raw material according to claim 1, wherein: one end of the propylene feeding line (11) is communicated with the third heat exchanger (6) through a pipeline, the other end of the propylene feeding line (11) is provided with a propylene storage tank, and the propylene storage tank is communicated with the propylene feeding line (11).
5. The apparatus for purifying butanol and octanol production raw material according to claim 1, wherein: one end of the water injection pipeline (12) is communicated with the propylene feeding line (11), the other end of the water injection pipeline (12) is provided with a water storage tank, and the water storage tank is communicated with the water injection pipeline (12).
6. The apparatus for purifying butanol and octanol production raw material according to claim 1, wherein: the first propylene purification tower (7) is internally provided with a first adsorption unit which comprises a plurality of adsorption layers, and the adsorption layers are fixedly connected with the first propylene purification tower (7).
7. The purification device for butanol and octanol production raw materials as claimed in claim 1, wherein: the inside second absorption unit that is provided with of second propylene purifying tower (8), second absorption unit and second propylene purifying tower (8) fixed connection.
8. The apparatus for purifying butanol and octanol production raw material according to claim 1, wherein: the first synthesis gas purification tower (2) is a vertical packed bed tower, a third adsorption unit is arranged in the first synthesis gas purification tower (2), and the third adsorption unit is fixedly connected with the first synthesis gas purification tower (2).
9. The purification device for butanol and octanol production raw materials as claimed in claim 1, wherein: the second synthetic gas purification tower (5) is a vertical packed bed tower, a plurality of beds are arranged inside the second synthetic gas purification tower (5), each bed is provided with a supporting plate at the bottom, and a pressing plate is arranged at the top of each bed.
10. The apparatus for purifying butanol and octanol production raw material according to claim 7, wherein: the bottom of the second propylene purification tower (8) is provided with a propylene collector, and the propylene collector is communicated with the second propylene purification tower (8) through a pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223200038.2U CN218653721U (en) | 2022-11-30 | 2022-11-30 | Butyl octanol raw materials for production purifier |
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| CN202223200038.2U CN218653721U (en) | 2022-11-30 | 2022-11-30 | Butyl octanol raw materials for production purifier |
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