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Propylene

Propylene, also known as propene, is a colorless, flammable gas with a distinctive odor.
It is a key building block in the petrochemical industry, serving as a precursor for a wide range of important chemicals and polymers.
Propylene is used in the production of polypropylene plastics, propylene oxide, cumene, and other valuable industrial compounds.
This versatile hydrocarbon plays a crucial role in the manufacturing of a variety of products, from packaging materials to automotive parts.
Researcers can leverage the PubCompare.ai platform to effortlessly locate and compare protocols from literature, preprints, and patents related to propylene, enhanceing the reproducibility and accuracy of their work in this vital area of chemistry and materials science.

Most cited protocols related to «Propylene»

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Publication 2010
Bath Calcium, Dietary HEPES propylene Sodium Azide Zinc
Data were obtained from 9139 subjects [4928 females aged 5–96 years (M = 31.8, SD = 18.9) and 4211 males aged 5–91 years (M = 30.7, SD = 17.7)]. Among them, 3432 (37.5%) had been included in a previous study to establish normative data [15 (link)]. According to the inclusion criteria for the respective studies, all subjects were healthy and none reported histories for any olfactory disturbances.
Odors were delivered using felt-tip pens (“Sniffin’ Sticks”) of approximately 14 cm length and an inner diameter of 1.3 cm. These pens carry a tampon soaked with 4 ml of liquid odorant. For odor presentation, the cap was removed from the pen for approximately 3 s, the pen’s tip brought in front of the subject’s nose and carefully moved from left to right nostril and backwards [3 (link)].
The threshold was obtained in a three alternative forced choice paradigm (3 AFC) where subjects were repeatedly presented with triplets of pens and had to discriminate one pen containing an odorous solution from two blanks filled with the solvent. Phenylethanol (dissolved in propylene glycol) or n-butanol (dissolved in water) were used, with both odorants having been found equivalent in olfactory sensitivity testing: scores obtained with both are correlated [17 (link)]. The highest concentration was a 4% odor solution. Sixteen concentrations were created by stepwise diluting previous ones by 1:2. Starting with the lowest odor concentration, a staircase paradigm was used where two subsequent correct identifications of the odorous pen or one incorrect answer marked a so-called turning point, and resulted in a decrease or increase, respectively, of concentration in the next triplet. Triplets were presented at 20 s intervals. The threshold score was the mean of the last four turning points in the staircase, with the final score ranging between 1 and 16 points.
The discrimination task used the same 3 AFC logic. Two pens of any triplet contained the same odorant, while the third pen smelled differently. Subjects were asked to indicate the single pen with a different smell. Within-triplet intervals were approximately 3 s. As the odors used in this subtest were more intense, between-triplets intervals were 20–30 s. The score was the sum of correctly identified odors. Hence, the scores in this task ranged from 0 to 16 points. Importantly, subjects were blindfolded for the threshold and discrimination tasks to avoid visual identification of target pens.
Odor identification comprised common and familiar odorants (recognized by at least 75% of the population). Subjects were presented with single pens and asked to identify and label the smell, using four alternative descriptors for each pen. Between-pen intervals were approximately 20–30 s. The total score was the sum of correctly identified pens, thus subjects could score between 0 and 16 points.
The final “TDI score” was the sum of scores for Threshold, Discrimination and Identification subtests, with a range between 1 and 48 points.
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Publication 2018
Butyl Alcohol Discrimination, Psychology Feelings Females Hypersensitivity Males Nose Odorants Odors Phenylethyl Alcohol Propylene Glycol Sense of Smell Solvents Triplets
All procedures followed the Institute of Laboratory Animal Research guidelines and were approved by the Animal Care and Use Committee of the National Institute of Mental Health. Transgenic mice expressing HSV-TK under the GFAP promoter were generated from a previously-generated plasmid28 (link) using standard techniques and bred on a mixed C57Bl/6:CD-1 background. Male v-WT and v-TK mice were treated with valganciclovir for 8 weeks (dexamethasone experiment), 10-19 weeks (endocrine), 12 weeks (behavior) or 4 weeks (histology; histology after 12 weeks in Supplementary Fig. 1), beginning at 8 weeks of age. Male C57Bl/6 mice were irradiated under pentobarbital anesthesia, as described previously29 (link), and tested 9 weeks later. For immunohistochemical analyses, mice were given BrdU 6 weeks (for PVN analysis) or 24 hours prior to sacrifice, brain sections were immunostained as previously described29 (link), and labeled cells were counted stereologically.
Serum corticosterone was measured by radioimmunoassay (MP Biomedicals) from submandibular blood samples obtained directly from the home cage condition or after exploration of a novel box, restraint, or isoflurane exposure. For the dexamethasone suppression test, dexamethasone (Sigma; 50 μg/kg in propylene glycol) or vehicle were injected 90 min prior to restraint, and blood was sampled immediately following 10 min restraint.
Behavioral tests were performed following 30 min of restraint or directly from the home cage. Different cohorts of mice were tested in the NSF test, elevated plus maze, forced swim test and sucrose preference test as previously described.12 (link), 18 (link), 21 , 30 (link) Statistical analyses were performed by t-test, log-rank test, or ANOVA with Fisher's LSD test for post hoc comparisons. Significance was set at P<0.05.
Publication 2011
Anesthesia Animals Animals, Laboratory Behavior Test BLOOD Brain Bromodeoxyuridine Cells Corticosterone Dexamethasone Elevated Plus Maze Test Glial Fibrillary Acidic Protein Isoflurane Males Mice, Inbred C57BL Mice, Laboratory Mice, Transgenic neuro-oncological ventral antigen 2, human Pentobarbital Propylene Glycol Radioimmunoassay Serum Sucrose System, Endocrine Valganciclovir

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Publication 2013
Animals Central Nervous System Ethanol Hypersensitivity Injections, Intraperitoneal Intrathecal Injection Lumbar Region Mice, House Needles Nitroglycerin Normal Saline Pharmaceutical Preparations Propylene Glycol Sumatriptan Topiramate
Yeast Strains and Constructs—The following yeast strains were used: BY4741 (MATa his3Δ1 leu2Δ met15Δ ura3Δ) and NDY257 (BY4741 rtn1::kanMX4 rtn2::kanMX4 yop1::kanMX) (6 (link)). Strains expressing GFP fusions to the chromosomal alleles of YOP1 and RTN1 were obtained from Invitrogen. The plasmid encoding Sec63-GFP (pJK59) has been previously described (12 (link)). To make the plasmid encoding Rtn1-GFP (pCV19), the SEC63 portion of pJK59 was removed by digestion with XbaI and XhoI. The RTN1 gene, including 400 bp upstream of the start site, was PCR-amplified from yeast chromosomal DNA and inserted into the same sites.
Mammalian Plasmid Constructs—HA-DP1 was described previously (6 (link)). HA-Rtn3c was cloned by PCR amplifying Rtn3c (NCBI accession number: BC036717) from mouse cDNA with primers containing an N-terminal HA tag and inserted into pcDNA3.1D (Invitrogen). For Rtn4a-GFP, human Rtn4a was PCR-amplified from Rtn4a-Myc (described in a previous study (6 (link))) and ligated into the pAcGFP-N1 backbone (Clontech) using the XhoI and KpnI restriction sites at the 5′ and 3′ ends, respectively. For GFP-Rtn3c, Rtn3c was PCR-amplified from HA-Rtn3c and ligated into the pAcGFP-C1 backbone (Clontech) using the XhoI and EcoRI restriction sites. To clone GFP-Rtn4HD, the region encoding amino acids 961–1192 was PCR-amplified from human Rtn4a-Myc and inserted into pAcGFP-C1 using the XhoI/EcoRI restriction sites. GFP-DP1 was subcloned by PCR-amplifying mouse DP1 from HA-DP1 (described in a previous study (6 (link))) and inserting into pAc-GFP C1 using SacI/BamHI restriction sites. For GFP-Climp63, Climp63 was PCR-amplified from mouse cDNA and cloned into pAcGFP-C1 using the XhoI/EcoRI sites. Climp63Δlum-GFP was cloned by PCR amplifying the region encoding amino acids 1–115 (as described in (13 (link))) from GFP-Climp63 and inserted into pAcGFP-N1 using XhoI/EcoRI restriction sites. LBR-GFP was PCR-amplified from plasmid containing human LBR (14 (link)) and cloned into pAcGFP-N1 using the XhoI/BamHI restriction sites. For GFP-Sec61β, human Sec61β was PCR-amplified from the pcDNA3.1/GFP-Sec61β construct described previously (6 (link)), and inserted into pAcGFP-C1 using the BglII/EcoRI restriction sites. RFP-Sec61β was subcloned from GFP-Sec61β using the same restriction sites as above and inserted into an mRFP1 vector (pEGFP-C1 vector backbone where pEGFP has been replaced with mRFP1).
Microscopy of Yeast—Yeast strains were grown in synthetic complete medium (0.67% yeast nitrogen base and 2% glucose) and imaged live at room temperature using an Olympus BX61 microscope, UPlanApo 100×/1.35 lens, QImaging Retiga EX camera, and IPlabs version 3.6.4 software.
Screen for Mutations in Yeast RTN1 That Affect Localization—Error-prone PCR on RTN1 was performed using the GeneMorphII Random Mutagenesis Kit (Stratagene). The product of this reaction and pJK59 cut with XbaI and XhoI were used to transform wild-type yeast. Transformants were visually screened for those that showed perinuclear GFP localization.
Tissue Culture, Indirect Immunofluorescence, and Confocal Microscopy of COS-7 Cells—Cells were grown at 37 °C with 5% CO2 in Dulbecco's modified Eagle's medium containing 10% fetal bovine serum and subcultured every 2–3 days. Transfection of DNA into cells was performed using Lipofectamine 2000 (Invitrogen). After 5 h of transfection, cells were split onto acid-washed No. 1 coverslips and allowed to spread for an additional 24–36 h before being processed for indirect immunofluorescence.
For immunofluorescence, transfected cells were fixed in PBS containing 4% paraformaldehyde (Electron Microscopy Sciences) for 15 min, washed twice, and permeabilized in 0.1% Triton X-100 (Pierce) in PBS for 5–15 min. Cells were washed twice again and then probed with primary antibodies for 45 min in PBS containing 1% calf serum, at the following concentrations: rat anti-HA antibody (Roche Applied Science) at 1:200 dilution; mouse anti-αtubulin (Sigma) at 1:500 dilution; and rabbit anti-calreticulin antibody (Abcam) at 1:500 dilution. Cells were washed three times in PBS, and then incubated with various fluorophore-conjugated secondary antibodies for an additional 45 min (Alexafluor 488 or 555 anti-mouse at 1:250 dilution, Alexafluor 647 anti-rabbit 1:500 dilution, and Alexafluor 488 anti-rat 1:200 dilution (all from Invitrogen)). Cells were then washed and mounted onto slides using Fluoromount-G mounting medium (Southern Biotech).
All imaging for indirect immunofluorescence was captured using a Yokogawa spinning disk confocal on a Nikon TE2000U inverted microscope with a 100× Plan Apo numerical aperture 1.4 objective lens, and acquired with a Hamamatsu ORCA ER cooled charge-coupled device camera using MetaMorph 7.0 software. For image presentation, brightness and contrast were adjusted across the entire image using Adobe Photoshop 7.0, and images were converted from 12 to 8 bits.
Transmission Electron Microscopy—COS-7 cells expressing GFP-Rtn4HD were sorted in a MoFlo cell sorter (Cytomation). The resulting cell pellet was fixed for 1 h in a mixture of 2.5% glutaraldehyde and 2% paraformaldehyde in 0.1 m sodium cacodylate buffer (pH 7.4), washed in 0.1 m cacodylate buffer, and postfixed with a mixture of 1% OsO4 and 1.5% KFeCN6 for 30 min. The pellet was then washed in water and stained in 1% aqueous uranyl acetate for 30 min followed by dehydration in grades of alcohol (50%, 70%, and 95%, 2 × 100%). Next, the pellet was infiltrated in a 1:1 mixture of propylene oxide and TAAB Peon (Maria Canada Inc.) for 2 h, placed in pure TAAB Epon in a silicon-embedding mold, and polymerized at 65 °C for 48 h. Ultrathin sections (∼60–80 nm) were cut on a Reichert Ultracut-S microtome, placed onto copper grids, and stained with 0.2% lead citrate. Specimens were examined on a Tecnai G Spirit BioTWIN transmission electron microscope, and images were acquired with a 2k AMT charge-coupled device camera.
Fluorescence Recovery after Photobleaching—Transfected COS-7 cells were imaged in phenol red-free HyQ DME (HyClone) supplemented with 25 mm Hepes, pH 7.4, and 1% fetal bovine serum. FRAP experiments were conducted on a Zeiss LSM 510 NLO laser scanning inverted microscope using a Plan-Neofluor 100×/1.3 oil objective with argon laser line 488 nm (optical slices <1.2 mm for COS-7 and 4.2 μm for yeast). Mammalian cell experiments were done at 37 °C using an objective heater (Bioptechs) and an enclosed stage incubator (Zeiss). LSM 510 software version 3.2 was used for image acquisition and analysis. Magnification, laser power, and detector gains were identical across samples.
For all mammalian experiments, COS-7 cells were treated with 0.5 μm nocodazole, and all data were collected during the first 5–30 min of nocodazole addition. For photobleaching all constructs, except for LBR-GFP, the tubular ER was magnified using the 3× zoom function so that individual tubules could be seen clearly. For LBR-GFP, the microscope was focused onto the bottom of the nuclear envelope. Images taken for 5-s prebleaching, whereupon a region of interest of 65 × 65 pixels was photobleached at 100% laser power. After the photobleaching, images were taken at 1-s intervals for 75–300 s. Yeast cells were treated similarly except that the region of interest was 17 × 17 pixels, and images were taken every 2–4 s at room temperature.
Raw data were quantitated using Zeiss LSM510Meta software. For analysis, the fluorescence intensity of three regions of interest was measured: the photobleached region (PR), a region outside of the cell to check for overall background fluorescence (BR), and a region within the cell that was not photobleached to check for overall photobleaching and fluorescence variation (CR), for the entire course of the experiment. Microsoft Excel was used to normalize the relative fluorescence intensity, I, for each individual FRAP experiment using Equation 1. For data presentation, the mean averages of the normalized data for each set of FRAP experiments were plotted using GraphPad Prism 5.0, and fluorescence recovery curves were shown for the first 80–140 s of each experiment. Estimated half-times of recovery and mobile fraction values were calculated using the standard Michaelis-Menten equation.
Sucrose Gradient Centrifugation—For yeast sucrose gradient analysis, crude membranes were isolated from yeast strains expressing GFP-fused proteins at endogenous levels as follows: 200 ml of culture were grown to OD ∼1, pelleted and then resuspended in TKMG lysis buffer (50 mm Tris, pH 7.0, 150 mm KCl, 2 mm MgCl2, 10% glycerol, 1 mm EDTA, 1 mm PMSF, 1 mm 4-(2-aminoethyl)benzenesulfonylfluoride hydrochloride), flash frozen in liquid nitrogen, and ground using a mortar and pestle. Cell debris was separated from the lysate by low speed centrifugation for 5 min at ∼2,000 × g. Membranes were then pelleted by ultracentrifugation for 15 min at 100,000 × g and solubilized in 200 μl of TKMG buffer containing 1% digitonin. Solubilized lysate was centrifuged for 10 min at 12,000 × g to separate out any remaining cell debris. 100-μl of lysate were run on 5–30% w/v sucrose gradients for 4 h at 166,000 × g at 25 °C on a Beckman TLS55 rotor. Twenty gradient fractions were collected from top to bottom and analyzed by SDS-PAGE and immunoblotting with anti-GFP antibody (Roche Applied Science). 50 mg of apoferritin, catalase, and aldolase was used as molecular weight standards.
Xenopus washed membrane fractions were prepared in MWB (50 mm Hepes, pH 7.5, 2.5 mm MgCl2, 250 mm sucrose, and 150 mm potassium acetate) as previously described (6 (link)), incubated for 60 min at 25 °C in MWB containing 200 mm KCl and 0.5 mm GTP, and then solubilized for 30 min at 25 °C with either 2% Nonidet P-40 or 1.25% digitonin. Samples were pelleted for 15 min at 12,000 rpm, and the soluble fraction was loaded onto a 10–30% w/v sucrose gradient made with MWB containing 200 mm KCl, 0.1 mm GTP, and either 0.1% Nonidet P-40 or 0.1% digitonin, respectively. The sucrose gradient was centrifuged for 3 h, 45 min at 55,000 rpm. Sixteen gradient fractions were collected and analyzed by SDS-PAGE and immunoblotted with antibody against Xenopus Rtn4 (described in a previous study (6 (link))).
For mammalian sucrose gradient analysis, COS-7 cells transiently transfected with HA-DP1 or GFP-Sec61β were harvested by scraping and then lysed and solubilized in HKME buffer (25 mm Hepes, pH 7.8, 150 mm potassium acetate, 2.5 mm magnesium acetate, 1 mm EDTA, and 2 mm PMSF) containing 1% digitonin for 1 h. The lysate was clarified by centrifugation at 10,000 × g for 10 min, and 100 μl of clarified lysate was sedimented on 5–30% w/v sucrose gradients under the same conditions as yeast. Fractions were analyzed by SDS-PAGE and immunoblotting with anti-HA antibody or anti-Sec61β antibody (described in a previous study (15 (link))).
Chemical Cross-linking Experiments—Yeast crude membrane fractions were resuspended in buffer containing 50 mm Hepes, pH 7.0, 150 mm KCl, and 1 mm PMSF. Ethylene glycobis(succinimidylsuccinate) (EGS, Pierce), was dissolved in anhydrous DMSO and diluted to the desired concentration. 1 μl of EGS was added into every 20 μl of protein-containing sample for 30 min at room temperature. The reactions were quenched for 15 min with 2 μl of 1 m Tris, pH 7.5. Samples were analyzed on a 4–20% SDS-PAGE and immunoblotted using standard procedures with mouse anti-His or rat anti-HA antibody conjugated to peroxidase (Sigma).
For mammalian cross-linking experiments, transfected COS-7 cells were grown in a 10-cm plate to ∼80% confluency and then lysed using a standard hypotonic lysis protocol. Briefly, cells were harvested in PBS, washed, incubated in hypotonic buffer (10 mm Hepes, pH 7.8, 10 mm potassium acetate, 1.5 mm magnesium acetate, 2 mm PMSF) for 10 min, and then passed through a 25-gauge syringe ten times. Nuclei and any remaining intact cells were separated from the lysate by centrifugation for 5 min at 3,000 × g, and the supernatant was then centrifuged for 10 min at 100,000 × g to pellet the membrane fraction. The membrane pellet was washed in HKM buffer (25 mm Hepes pH 7.8, 150 mm potassium acetate, 2.5 mm magnesium acetate, and 2 mm PMSF), repelleted at 100,000 × g, and resuspended to a final volume of 60 μl in HKM buffer. 10-μl membrane aliquots were used for each cross-linking reaction using the same conditions as above. Samples were analyzed on a 4–20% SDS-PAGE and immunoblotted using standard procedures with anti-HA antibody.

Rtn1p and Yop1p have slow diffusional mobility in the ER of yeast cells. A, typical FRAP of Sec63-GFP or Rtn1-GFP in S. cerevisiae cells expressed at endogenous levels. Images were taken before and then after the photobleach for the times indicated. The boxed region shows the area that was photobleached. B, fluorescence intensities normalized to prebleach values of FRAP analyses on yeast Sec63-GFP, Rtn1-GFP, and Yop1-GFP were plotted over time. Error bars indicate ± S.E.; n = 4 cells. C, fluorescence intensities normalized to prebleach values plotted over time of FRAP analyses on yeast Rtn1p in ATP-depleted (green) or non-depleted (orange) cells, compared with that of Sec63p-GFP (ATP depleted in blue; non-depleted in red). Error bars indicate ± S.E., n = 4 cells.


ATP Depletion Experiments—For yeast experiments, ATP was depleted by the addition of 10 mm 2-deoxy-d-glucose and 10 mm sodium azide (both from Sigma) for 2–5 min, and FRAP experiments were performed using the same parameters as described above. Similarly, for mammalian cell experiments, COS-7 cells were depleted of ATP as follows: transfected cells were washed twice in Opti-Mem serum-free media (Invitrogen) and then incubated with 50 mm 2-deoxy-d-glucose and 0.02% sodium azide in glucose-free imaging buffer (50 mm Hepes, pH 7.4, 150 mm potassium acetate, 2.5 mm magnesium acetate, and 1% fetal bovine serum). FRAP experiments were conducted in the same medium and completed within 5–30 min of treatment using the same parameters as above.
Publication 2008

Most recents protocols related to «Propylene»

Experiments were carried out to polymerize propylene in a slurry using a catalyst of TiCl4, DBP (dibutylphthalate), and MgCl2. The process was carried out in a 1 L stainless steel reactor with a stirrer that rotates at 360 revolutions per minute. The polymerization medium that was used was heptane, and 500 mL of heptane was introduced into the reactor. The propylene was saturated at a pressure of 0.3 mega Pascals (MPa) to initiate polymerization for 30 min. Then, specific amounts of an aluminum alkyl activator and CMDMS (an external donor) were added to the reactor, maintaining an Al/Si molar ratio of 4.7. Next, a specified amount of the catalyst was injected into the reactor to start the polymerization reaction at the desired temperature. CO2, CO, and O2 were added to the propylene supply line (look at Table 1).
After the polymerization was complete, acetone was added to stop the process, and then the suspension was transferred to a receiving flask that was kept under a nitrogen (N2) atmosphere. The synthesized powder was washed three times with 200 mL of heptane and then dried in a vacuum at room temperature. The resulting polymer was stored under dark, nitrogen, and temperature-controlled conditions. It is essential to highlight that all the procedure steps were carried out very carefully in a nitrogen atmosphere to avoid air.
The standard polymerization conditions were as follows: polymerization temperature = 70 °C, amount of catalyst = 5 Kh/h, type of activator = TEAL, concentration of activator = 0.25 Kh/h, 30 g/h of H2, and 1.2 TM/h of propylene at a pressure of 27 bar.
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Publication 2024

Example 3

The test was conducted in accordance with the process flow shown in FIG. 3 using Feedstock oil C as a starting material for catalytic conversion on an equal-diameter riser reactor. Feedstock oil C was contacted with Catalyst C, and reacted in the riser reactor under conditions including a reaction temperature of 530° C., a reaction time of 3.5 seconds, a catalyst-to-oil weight ratio of 8, and a steam-to-oil weight ratio of 0.1 to obtain a spent catalyst and a reaction product. The spent catalyst was regenerated, and the regenerated catalyst was recycled to the riser reactor as the catalytic conversion catalyst. The reaction product was split according to distillation range in a product separation device to obtain dry gas, ethylene, propylene, propane, a fraction comprising C4 olefin (with a C4 olefin content of 85.0 wt %), butane, gasoline, diesel oil and slurry oil.

The fraction comprising C4 olefin was fed to an oligomerization reactor for oligomerization, and the fraction comprising C12 olefin (with a C12 olefin content of 85.3 wt %) separated by a rectifying column was recycled to the riser reactor. The C12 olefin recycled to the riser reactor for further cracking accounted for 14.17 wt % of the total catalytic conversion feedstock. The operating conditions and product distribution are listed in Table 5.

The operation was substantially the same as in Example 3, except that the catalytic conversion product was split according to distillation range in the product separation device to obtain dry gas, liquefied gas, propylene, gasoline, diesel oil and slurry oil, and the recycling of the catalytic conversion product was not performed. The operating conditions and product distribution are listed in Table 5.

TABLE 5
Operating conditions and results of
Example 3 and Comparative Example 3
Comparative
ItemExample 3Example 3
Feedstock oilCC
Operating conditions (catalytic conversion reaction device)
ReactorRiser reactorRiser reactor
CatalystCC
Reaction temperature, ° C.530530
Reaction time, second3.53.5
Steam/feedstock oil weight ratio0.10.1
Catalyst/feedstock oil weight ratio88
Operating conditions (oligomerization reactor)
CatalystE/
Temperature of C4 olefin200/
oligomerization, ° C.
Pressure of C4 olefin oligomerization,2/
MPa
Weight hourly space velocity of C41/
olefin oligomerization, h−1
Product distribution, wt %
Dry gas3.753.72
Methane0.890.87
Ethane0.680.66
Liquefied gas22.7523.10
Propylene13.858.56
Propylene/propane/5.3
Isobutene/isobutane/1.0
Gasoline43.7043.51
Diesel oil19.5519.49
Slurry oil3.533.51
Coke6.726.67
Total100.00100.00

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Patent 2024
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Example 2

The test was conducted using Feedstock oil B as the feedstock for catalytic conversion, on a composite reactor as shown in FIG. 2 comprising a riser and a dense phase bed connected in series. The Feedstock oil B was contacted with Catalyst B, reacted in the riser unit under conditions including a reaction temperature of 650° C., a reaction time of 0.8 second, a catalyst-to-oil weight ratio of 20, and a steam-to-oil weight ratio of 0.8; the resulting reaction stream was passed to the dense phase bed unit for further reaction at a reaction temperature of 580° C. and a weight hourly space velocity of 10 h−1 to obtain a spent catalyst and a reaction product. The spent catalyst was regenerated, and the regenerated catalyst was recycled to the riser unit as the catalytic conversion catalyst. The reaction product was split according to distillation range in a product separation device to obtain dry gas, ethylene, propylene, propane, a fraction comprising C4 olefin (with a C4 olefin content of 84.8 wt %), butane, gasoline, diesel oil and slurry oil.

The fraction comprising C4 olefin was fed to an oligomerization reactor for oligomerization, and the fraction comprising C12 olefin (with a C12 olefin content of 85.1 wt %) separated by a rectifying column was recycled to the dense phase bed unit. The C12 olefin introduced into the dense phase bed unit for further cracking accounted for 15.5 wt % of the total catalytic conversion feedstock. The operating conditions and product distribution are listed in Table 4.

The operation was substantially the same as in Example 2, except that the catalytic conversion product was separated and split to obtain dry gas, liquefied gas, propylene, gasoline, diesel oil and slurry oil, and the recycling of the catalytic conversion product was not performed. The operating conditions and product distribution are listed in Table 4.

TABLE 4
Operating conditions and results of
Example 2 and Comparative Example 2
Comparative
ItemExample 2Example 2
Feedstock oilBB
Operating conditions (catalytic conversion reaction device)
ReactorRiser + dense Riser + dense
phase bedphase bed
Riser unit
CatalystBB
Reaction temperature, ° C.650650
Reaction time, second0.80.8
Steam/feedstock oil weight ratio0.80.8
Catalyst/feedstock oil weight ratio20.020.0
Dense phase bed unit
Reaction temperature, ° C.580580
Weight hourly space velocity, h−11010
Operating conditions (oligomerization reactor)
CatalystE/
Temperature of C4 olefin200 /
oligomerization, ° C.
Pressure of C4 olefin oligomerization,2/
MPa
Weight hourly space velocity of C41/
olefin oligomerization, h−1
Product distribution, wt %
Dry gas12.5111.91
Methane3.323.24
Ethane2.342.33
Liquefied gas40.4342.22
Propylene25.6519.30
Propylene/propane/6.34
Isobutene/isobutane/2.03
Gasoline27.3126.60
BTX7.617.53
Diesel oil6.836.69
Slurry oil6.396.37
Coke6.536.21
Total100.00100.00

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Patent 2024

Example 1

This example was conducted in accordance with the process flow shown in FIG. 1, using Feedstock oil A directly as a feedstock for catalytic conversion, on a pilot plant of diameter-transformed riser reactor. Feedstock oil A was fed to the bottom of a first reaction zone 9, contacted with Catalyst A at the bottom of the first reaction zone 9 and subjected to catalytic conversion reaction sequentially in the first reaction zone 9 and a second reaction zone 8. The resulting reaction product and spent catalyst deposited with carbon were separated in a disengager, and the reaction product was split according to distillation range in a product separation device to obtain dry gas, ethylene, propylene, propane and a fraction comprising C4 olefin (with a C4 olefin content of 85.9 wt %), butane, gasoline, a light cycle oil fraction having a distillation range of 200-260° C., and a FGO fraction having a distillation range of >260° C.

The fraction comprising C4 olefin was fed to an oligomerization reactor for oligomerization, and the fraction comprising C12 olefin (with a C12 olefin content of 85.2 wt %) separated by a rectifying column was recycled to the second reaction zone 8; the light cycle oil fraction having a distillation range of 200-260° C. was recycled to the first reaction zone 9 for reuse, the FGO fraction having a distillation range >260° C. was subjected to a hydrotreatment under conditions including a hydrogen partial pressure of 18.0 MPa, a reaction temperature of 350° C., a hydrogen-to-oil volume ratio of 1500 and a volume space velocity of 1.5 h−1, and the hydrogenation product was recycled to the first reaction zone 9 for catalytic conversion reaction. The C12 olefin introduced in the second reaction zone 8 accounted for 18.9 wt % of the total catalytic conversion feedstock. The operating conditions and product distribution are listed in Table 3.

The operation was substantially the same as in Example 1, except that a conventional catalytic cracking catalyst D was used and the product was split as required in the conventional catalytic cracking process to obtain dry gas, liquefied gas, propylene, gasoline, diesel oil and slurry oil, and no recycle of the catalytic conversion product was carried out. The operating conditions and product distribution are listed in Table 3.

The operation was substantially the same as in Example 1, except that the separated C4 olefin-containing fraction (with a C4 olefin content of 85.7%) was fed to the oligomerization reactor for oligomerization, and the C8 olefin-containing fraction (with a C8 olefin content of 84.9 wt %) separated by the rectifying column was recycled to the second reaction zone, and the C8 olefin accounted for 18.8 wt % of the total catalytic conversion feedstock. The operating conditions and product distribution are listed in Table 3.

TABLE 3
Operating conditions and results of Example 1, Comparative
Examples 1-a and 1-b
ComparativeComparative
ItemExample 1Example 1-aExample 1 b
Feedstock oilFeedstock FeedstockFeedstockFeedstock
oiloiloiloil
AA*AA
Operating conditions (catalytic conversion reaction device)
ReactorDual-Dual-Dual-Dual-
diameterdiameterdiameterdiameter
riserriserriserriser
CatalystAADA
Riser outlet500500500500
temperature, ° C.
Temperature of550/500550/500550/500550/500
reaction zone I/II,
° C.
Reaction time of1.0/4.71.0/4.71.0/4.71.0/4.7
reaction zone I/II,
second
Catalyst-to-oil5.0/6.55.0/6.55.0/6.55.0/6.5
weight ratio of
reaction zone I/II
Steam/feedstock oil0.100.100.100.10
weight ratio
Operating conditions (oligomerization reactor)
CatalystE//E
Temperature of C4200//120
olefin
oligomerization, ° C.
Pressure of C42//1
olefin
oligomerization,
MPa
Weight hourly1//1
space velocity of
C4 olefin
oligomerization, h−1
Operating conditions (hydrotreating reactor)
CatalystF//F
Temperature, ° C.350//350
Hydrogen partial18.0//18.0
pressure, MPa
Volume space1.5//1.5
velocity, h−1
Hydrogen-to-oil1500//1500
volume ratio
Product distribution, wt %
Dry gas3.623.303.013.54
Methane0.430.400.510.51
Ethane0.330.310.380.38
Liquefied gas35.2528.0917.5133.94
Propylene25.6812.115.122.67
Propylene/propane/3.93.0/
Isobutene/isobutane/1.80.7/
Gasoline51.5137.3948.8152.93
Diesel oil18.9018.92
Slurry oil3.643.00
Coke9.628.688.759.59
Total100.00100.00100.00100.00
*Data of Example 1 in column 2 are operating conditions and results for the case where the catalytic conversion reaction was carried out only in the diameter-transformed riser reactor and the resulting catalytic conversion product was not recycled.

Example 4

The test was conducted using Feedstock oil C as a feedstock for catalytic conversion on a system of double riser reactors as shown in FIG. 4. Feedstock oil C was contacted with Catalyst C, and reacted in a first riser reactor at a reaction temperature of 530° C., a reaction time of 3.5 seconds, a catalyst-oil weight ratio of 8 and a steam-to-oil weight ratio of 0.10 to obtain a spent catalyst and a reaction product. The spent catalyst was regenerated, and the regenerated catalyst was recycled to the first riser reactor as the catalytic conversion catalyst. The resulting reaction product was split according to distillation range in a product separation device to obtain dry gas, ethylene, propylene, propane, butane, a fraction comprising C4 olefin (with a C4 olefin content of 85.3 wt %), gasoline, diesel oil and slurry oil.

The fraction comprising C4 olefin was fed to an oligomerization reactor 44 for oligomerization in accordance with the process flow shown in FIG. 4, a fraction comprising C12 olefin (with a C12 olefin content of 85.0 wt %) was separated by a rectifying column, and the fraction comprising C12 olefin was fed to the bottom of the second riser reactor for reaction. The C12 olefin introduced into the second riser reactor accounted for 15.9 wt % of the total catalytic conversion feedstock, and the reaction was conducted at a reaction temperature of 530° C., a reaction time of 2.0 seconds, a catalyst-to-oil weight ratio of 8, and a steam-to-oil weight ratio of 0.10. The operating conditions and the product distribution of the final product obtained by combining the reaction products of the first riser reactor and the second riser reactor are listed in Table 6.

TABLE 6
Operating conditions and results of Example 4
ItemExample 4
Feedstock oilC
Operating conditions (catalytic conversion reaction device)
ReactorDouble risers
connected in parallel
CatalystC
Outlet temperature of the 530/530
first/second riser, ° C.
Reaction time of the 3.5/2.0
first/second riser, second
Weight ratio of catalyst/feedstock oil8
Weight ratio of steam/feedstock oil0.10
Operating conditions (oligomerization reactor)
CatalystE
Temperature of C4 200
olefin oligomerization, ° C.
Pressure of C4 olefin 2
oligomerization, MPa
Weight hourly space velocity of C4 1
olefin oligomerization, h−1
Final product distribution, wt %
Dry gas3.83
Liquefied gas21.46
Propylene15.76
Gasoline43.50
Diesel oil20.31
Slurry oil3.82
Coke7.08
Total100.00

As can be seen from a comparison of the results of the above examples and comparative examples, the process and system of the present application provides a higher propylene yield by oligomerizing C4 olefin to C12 olefin and recycling the resulting C12 olefin. In addition, the results in Table 3 also show that the catalytic conversion reaction of Example 1 can provide a lower alkane yield and a higher propylene yield by itself, as compared to Comparative Example 1, and the propylene yield can be further greatly increased by the oligomerization of C4 olefin and the recycle of C12 olefin.

The present application is illustrated in detail hereinabove with reference to preferred embodiments, but is not intended to be limited to those embodiments. Various modifications may be made following the inventive concept of the present application, and these modifications shall be within the scope of the present application.

It should be noted that the various technical features described in the above embodiments may be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, various possible combinations are not described in the present application, but such combinations shall also be within the scope of the present application.

In addition, the various embodiments of the present application can be arbitrarily combined as long as the combination does not depart from the spirit of the present application, and such combined embodiments should be considered as the disclosure of the present application.

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Patent 2024

Example 2

Example 2 was conducted at a pilot plant having the first reactor configuration and characteristics of steam catalytic cracking reactor 180 illustrated in FIG. 2. In Example 2, the steam catalytic cracking reactor of the present disclosure was operated in the propylene-selective mode to obtain light olefins from a hydrocarbon feed.

The hydrocarbon feed comprised 20 wt. % naphtha preheated to from 93° C. to 205° C. and 80 wt. % vacuum gas oil heated to from 370° C. to 590° C. was passed to a fixed bed steam catalytic cracking reactor. The hydrocarbon feed was preheated and the preheated feed at 70° C. was introduced to the reactor at space velocity of 0.5 hourly (h−1) and steam was injected at space velocity of 1 hourly (h−1). The steam to oil volume ratio was 2 to 1. The steam catalytic cracking was carried out in the steam catalytic cracking reactor loaded with nano ZSM-5 zeolite bounded with 40 wt. % alumina binder. The catalyst was loaded into the steam catalytic cracking reactor forming a cylindrical catalyst bed arranged with a height of 4 units and diameter of 2 units. The catalyst loading height to diameter ratio was 2 to 1, for a ratio of height HC to inside diameter ID of 2. The inert carrier pre-heating zone of the steam catalytic cracking reactor was loaded with silica carbide. The inert carrier pre-heating loaded volume to catalyst loaded volume ratio was 2 to 1. The catalyst bed zone and the inert carrier pre-heating zone were operated at 575° C.

As shown in Table 4, the steam catalytic cracking process operated in the propylene-selective mode achieved high conversion. High yield of olefins 49 wt. % with a yield ratio of propylene/ethylene of 1.87 was obtained.

TABLE 4
Composition of steam catalytic
cracking effluent from Example 2
Example 2
ConsistentYield (wt. %)
Naphtha10.4 
Gas oil13.2 
VGO16.1 
Olefins49  
Ethylene10.8 
Propylene20.3 
Butenes17.9 
P/E1.9
LPG2.9
Dry gas7.1

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Patent 2024

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