GB2024245A - Production of gaseous and liquid fuels and coke from scrap rubber - Google Patents
Production of gaseous and liquid fuels and coke from scrap rubber Download PDFInfo
- Publication number
- GB2024245A GB2024245A GB7919438A GB7919438A GB2024245A GB 2024245 A GB2024245 A GB 2024245A GB 7919438 A GB7919438 A GB 7919438A GB 7919438 A GB7919438 A GB 7919438A GB 2024245 A GB2024245 A GB 2024245A
- Authority
- GB
- United Kingdom
- Prior art keywords
- rubber
- scrap rubber
- coke
- gaseous
- liquid fuels
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 229920001971 elastomer Polymers 0.000 title claims abstract description 39
- 239000005060 rubber Substances 0.000 title claims abstract description 39
- 239000000446 fuel Substances 0.000 title claims description 18
- 239000007788 liquid Substances 0.000 title claims description 14
- 239000000571 coke Substances 0.000 title description 19
- 238000004519 manufacturing process Methods 0.000 title description 6
- 238000000034 method Methods 0.000 claims abstract description 29
- 239000010779 crude oil Substances 0.000 claims abstract description 18
- 239000000725 suspension Substances 0.000 claims abstract description 4
- 238000005336 cracking Methods 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 238000000638 solvent extraction Methods 0.000 claims description 2
- 238000004939 coking Methods 0.000 abstract description 8
- 239000003921 oil Substances 0.000 abstract description 5
- 230000003111 delayed effect Effects 0.000 abstract 1
- 238000004227 thermal cracking Methods 0.000 abstract 1
- 238000005292 vacuum distillation Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 20
- 238000010438 heat treatment Methods 0.000 description 7
- 239000005864 Sulphur Substances 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 238000000197 pyrolysis Methods 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229920001195 polyisoprene Polymers 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 1
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N N-phenyl amine Natural products NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 229940063718 lodine Drugs 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229920003052 natural elastomer Polymers 0.000 description 1
- 229920001194 natural rubber Polymers 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Wood Science & Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Processing Of Solid Wastes (AREA)
- Coke Industry (AREA)
Abstract
Scrap rubber, such as used tyres, inner tubes and belts, is dissolved or suspended in a residue from the processing of crude oil (such as a vacuum distillation residue) and submitted to thermal cracking at 450 to 580 DEG C and a pressure of from 0.5 to 11 atmospheres gauge. The solution or suspension can be produced by extracting particulate rubber with the oil at 100-500 DEG C and the extract subjected to a delayed coking process.
Description
SPECIFICATION
Process for producing gaseous and liquid fuels from waste rubber products
This invention relates to a process for producing gaseous and liquid fuels from waste rubber products.
More specifically the invention relates to a process for converting scrap rubber, such as used tyres, inner tubes, belts, and other waste material, into gaseous and liquid fuels, and coke, using waste products from processing of crude oil.
Known methods of utilizing scrap rubber involve dissolving thereof in residues from the processing of crude oil. This liquefaction is conducted using various types of solvents at temperatures up to 400"C. The product of this process is used as binding agents of various kinds and as additives to asphalts.
Another known method of utilizing scrap rubber requires the decomposition thereof by destructive distillation in a retort at a temperature of from 400 to 5600C or 750 to 1 0000C. This process of destructive distillation is conducted at normal or reduced pressure, with steam or in inert atmosphere. The distillates obtained are employed as solvents and softeners for natural and synthetic rubbers. Liquid fractions obtained by such processes of decomposition (pyrolysis) have not found any widespread application for the production of engine fuels because their composition makes hydrogenation very difficult. They also have an unpleasant odour.
The application of the process of this invention for conversion of scrap rubber gives fuels of much better composition thus enabling considerably simpler final processing whereby their unpleasant odour disappears completely.
In course of testing carried out, an increased yield of lighter fuels and higher quality products, has been found in the comparison of processing the crude oil residues alone or the pyrolysis of scrap tyre rubber alone.
An object of the invention is to obviate or mitigate the aforesaid disadvantages.
According to the present invention there is provided a process for converting scrap rubber into gaseous and liquid fuels comprising dissolving or suspending the scrap rubber in residues from the processing of crude oil and thermally cracking the rubber and residue at a temperature of from 450 to 580"C and at a pressure of from 0.5 to 11 atmospheres gauge.
The first step of the process involves liquefaction of scrap rubber, preferably in amounts of from 15 to 50% by weight, by dissolution in residues from the processing of crude oil. The liquefaction may be conducted gradually using a solvent extraction technique and forming suspensions at temperatures of from 100 to 500"C.
The scrap rubber dissolved or liquefied in this way is then submitted to cracking to coke at a temperature of from 450 to 580"C and pressure of from 0.5 to 11 atmospheres guage.
The processing of scrap rubber by the method of cracking to coke together with products and/or residues of crude oil refining makes possible a broad utilization of said scraps for production of gaseous and liquid fuels (thereunder of engine fuels) and of coke, constituting conditions for utilization of all the disposable rubber scraps into such valuable products as engine fuels.
Unexpectedly it has been found that the scrap rubber added to the residual products of crude oil refining in amount of from 15 to 50% by weight shows an advantageous influence on the quality of final products obtained in processes of liquefaction of rubber and subsequent cracking. Caoutchoucs constituting the basic materials for production of tyres are composed of hydrocarbons wherein the ratio of hydrogen to carbon is higher than in certain residues of processing of the crude oil, which makes them excellent as raw material for production of fuels by the process of this invention. An addition of said raw materials to the residues of crude oils increases the ratio of hydrogen to carbon in said residues and makes them more appropriate for production of fuels after the method of cracking to coke.The introduction of scrap rubber with a content of sulphur not exceeding about 25% by weight makes it possible to reduce the content of sulphur in the coke obtained in this process in relation to cokes obtained from high-sulphur residues of crude oils.
The use of residues from processing the crude oils to liquefy the scrap rubber facilitates the process of thermal decomposition of hydrocarbons constituting the caoutchouc.
The products of processing the scrap rubber with crude oil residues are engine fuels and electrode coke of high quality with a low sulphur content.
The quality of the products can be controlled according to requirements by varying the amount of scrap rubber used within the limits of from 15 to 50% by weight in relation to the entire mass.
An embodiment of the process of this invention will now be described with reference to the accompanying block diagram.
The scrap rubber and the vacuum residue from crude oil processing are supplied to the dissolving unit 1 wherein the rubber dissolves in the hot residue at a suitable temperature resulting in a homogeneous liquid known as a destruct.
The required temperature is maintained in the dissolving unit 1 and a heating unit 2.
The product obtained is then heated in the membraneless heat exchange unit 3 and then in the membrane-equipped heating unit 4 and supplied to the coking unit 5 wherein coke is produced and simultaneously the educed water vapour phase is passed to the condensation and separation unit 6.
The liquid and gaseous products obtained in this unit are final products of the plant wherefrom they are discharged to tanks.
The coking unit 5 is divided into sections operating in cycles, and on depositing the coke in one section it is cooled down and the coke is discharged therefrom and classified. Meanwhile the other sections continue to operate.
The process may be conducted in such way that the scrap rubber is charged into extractors of a special type, wherethrough there are passed residue products of processing of the crude oil, heated to an appropriate temperature and which are capable of dissolving the rubber. The extraction temperature is increased gradually, charging the extractors with hotter and hotter solvent and/or solution of rubber in solvents. By carrying out the extraction in this way the entire soluble portion of the rubber is dissolved in petroleum products, and the substances able to form suspensions form a dispersed phase in said solutions.
The process of extraction is continued until solutions of suitable rubber content are obtained which are, however, able of being pumped to the subsequent phases of the processing.
The product prepared in this way is then heated in heat exchangers and/or in a furnace, and supplied to the bottom of the heating column.
The residue from the column bottom is heated in a pipe furnace to a temperature whereat a cracking reaction occurs, whereafter it is supplied to the coking chambers wherein cracking reaction is completed and coke is formed.
The vapours from the top of the coking chambers are also supplied to the fractionating column. Therefrom gas, petrols as well as fuel and heating oils are discharged.
The coke produced in the chambers is discharged by known methods.
Examples of the present invention will now be described by way of illustration.
EXAMPLE I
500 kg of rubber scraps were mixed with 500 kg of vacuum remainder from Romashkhin crude oil, and the whole was heated to a temperature of 250"C under agitation till liquefaction. The liquefied destruct had the following properties:
Specific gravity 1.11 g/cm3
Flash point (open/closed crucible) 258/152"C Content of benzene-insoluble compounds 16.0%
Ash content 2.3%
Sulphur content 2.4%
Coking residue 30.9%
Softening point 47.3 C The destruct was introduced into a retort where it was heated to the temperature of 450"C and maintained at that temperature for the entire time of discharging the gaseous and liquid fractions. On finishing the separation of liquid and gaseous products the coke contained in the retort was heated to the temperature of 550"C and maintained at that temperature, and for the entire time purged with overheated steam for 2 hours.
Liquid products were refluxed in a cooler and submitted to a distillation. The remaining mass of coke was cooled to ambient temperature and discharged from the retort.
The following products were obtained:
Gaseous fraction (heating gas) 183
Petrol fraction to 180"C 160
Fuel oil fraction to 2850C 157
Heating oil fraction, 258 to 2850C 55
Coke 380
Loses (together with fractionating) 65
Total: 1000 kg
The products had the following properties::
FRACTION
Units upto 180- 258 180 C 250"C 285"C Coke
Specific gravity kg/m3 893.2 881.2 914.4 -
Setting point "C -72 -21 +4 -
Acid number KOH/g 0.02375 0.06025 -- -lodine number g J/100g 79.40 43.845 43.808 -
Aniline point C 31.9 45.4 54.2 -
Sulphur content % 0.7055 1.557 1.811 4.288
Coke content % 0.01115 0.0154 0.0300 92.0
Ash content % -- -- -- 3.53 EXAMPLE II 150 kg of rubber scraps were mixed with 850 kg of the remainder from light Arabian crude oil, and processed further as described in Example 1.A A rubber destruct was obtained having the following properties: :
Specific gravity 1.10 g/cm3
Flash point (open crucible) 230"C Ash content 2.0%
Sulphur content 2.23%
Coking residue 28.5%
The destruct was submitted to coking as per Example I, whereafterthe following products were obtained:
Gaseous fraction 190
Petrol fraction up to 180 C 165
Fuel oil fraction up to 285CC 155
Heating oil fraction (plus slop oil) 55
Coke 370
Losses (together with frationating) 65
Total: 1000kg
Claims (5)
1. A process for converting scrap rubber into gaseous and liquid fuels comprising dissolving or suspending the scrap rubber in residues from the processing of crude oil and thermally cracking the rubber and residue at a temperature of from 450 to 580"C and at a pressure of from 0.5 to 11 atmospheres gauge.
2. A process according to claim 1, in which scrap rubber in amount of from 15 to 50% by weight is dissolved in the residues.
3. A process according to claim 1 or 2, in which the scrap rubber is suspended in the residues by a solvent extraction technique and the suspension is formed at a temperature of from 100 to 5000C.
4. A process for converting scrap rubber to gaseous and liquid fuels according to Example I or Example II hereinbefore.
5. Gaseous and liquid fuels whenever produced by the process claimed in any of claims 1 to 4.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PL1978207371A PL115716B1 (en) | 1978-06-05 | 1978-06-05 | Method of conversion of rubber scraps into gas and liquid fuels using cracking method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2024245A true GB2024245A (en) | 1980-01-09 |
| GB2024245B GB2024245B (en) | 1982-12-15 |
Family
ID=19989717
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB7919438A Expired GB2024245B (en) | 1978-06-05 | 1979-06-04 | Production of gaseous and liquid fuels and coke from scraprubber |
Country Status (9)
| Country | Link |
|---|---|
| JP (1) | JPS54159472A (en) |
| CS (1) | CS214786B2 (en) |
| DD (1) | DD144171A5 (en) |
| DE (1) | DE2922553A1 (en) |
| FR (1) | FR2431528A1 (en) |
| GB (1) | GB2024245B (en) |
| IT (1) | IT1121251B (en) |
| PL (1) | PL115716B1 (en) |
| RO (1) | RO78651A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2129009A (en) * | 1982-02-17 | 1984-05-10 | Rupert Holl | Process to increase the yield of pyrolysis oil and to shorten the duration of the pyrolysis |
| CN109355086A (en) * | 2018-12-17 | 2019-02-19 | 陕西延长石油（集团）有限责任公司 | A kind of method that waste tire produces fuel oil, coke |
| WO2023117516A1 (en) * | 2021-12-20 | 2023-06-29 | Sabic Global Technologies B.V. | Process for conversion of waste plastics into chemicals |
| WO2023117515A1 (en) * | 2021-12-21 | 2023-06-29 | Sabic Global Technologies B.V. | Process for conversion of waste plastics into chemicals. |
| EP4600329A1 (en) | 2024-02-08 | 2025-08-13 | Indian Oil Corporation Limited | A process of conversion of waste tyre oil to chemicals |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4686007A (en) * | 1983-06-17 | 1987-08-11 | Belorussky Politekhnichesky Institut | Method of thermally decomposing polymeric material |
| DE3326284C2 (en) * | 1983-07-21 | 1985-08-14 | Fried. Krupp Gmbh, 4300 Essen | Process for the production of liquid hydrocarbons |
| WO1995009901A1 (en) * | 1993-10-04 | 1995-04-13 | Texaco Development Corporation | Liquefaction and partial oxidation of plastic materials |
| US5464503A (en) * | 1993-10-28 | 1995-11-07 | Texaco Inc. | Tire liquefying process reactor discharge system and method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2357630A1 (en) * | 1976-07-05 | 1978-02-03 | Erap | Catalytic cracking in presence of rubber pyrolysis oil - from waste tyre material, giving improved yield of gasoline |
-
1978
- 1978-06-05 PL PL1978207371A patent/PL115716B1/en unknown
-
1979
- 1979-06-01 CS CS793790A patent/CS214786B2/en unknown
- 1979-06-01 DE DE19792922553 patent/DE2922553A1/en not_active Withdrawn
- 1979-06-04 IT IT23266/79A patent/IT1121251B/en active
- 1979-06-04 RO RO7997725A patent/RO78651A/en unknown
- 1979-06-04 GB GB7919438A patent/GB2024245B/en not_active Expired
- 1979-06-04 JP JP6981279A patent/JPS54159472A/en active Pending
- 1979-06-05 FR FR7914324A patent/FR2431528A1/en active Pending
- 1979-06-05 DD DD79213409A patent/DD144171A5/en unknown
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2129009A (en) * | 1982-02-17 | 1984-05-10 | Rupert Holl | Process to increase the yield of pyrolysis oil and to shorten the duration of the pyrolysis |
| CN109355086A (en) * | 2018-12-17 | 2019-02-19 | 陕西延长石油（集团）有限责任公司 | A kind of method that waste tire produces fuel oil, coke |
| WO2023117516A1 (en) * | 2021-12-20 | 2023-06-29 | Sabic Global Technologies B.V. | Process for conversion of waste plastics into chemicals |
| WO2023117515A1 (en) * | 2021-12-21 | 2023-06-29 | Sabic Global Technologies B.V. | Process for conversion of waste plastics into chemicals. |
| EP4600329A1 (en) | 2024-02-08 | 2025-08-13 | Indian Oil Corporation Limited | A process of conversion of waste tyre oil to chemicals |
Also Published As
| Publication number | Publication date |
|---|---|
| DD144171A5 (en) | 1980-10-01 |
| FR2431528A1 (en) | 1980-02-15 |
| CS214786B2 (en) | 1982-05-28 |
| PL207371A1 (en) | 1979-12-17 |
| IT1121251B (en) | 1986-04-02 |
| RO78651A (en) | 1982-03-24 |
| JPS54159472A (en) | 1979-12-17 |
| PL115716B1 (en) | 1981-04-30 |
| IT7923266A0 (en) | 1979-06-04 |
| DE2922553A1 (en) | 1979-12-13 |
| GB2024245B (en) | 1982-12-15 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PG | Patent granted |