text:
|Publication number||US3283028 A|
|Publication date||Nov 1, 1966|
|Filing date||Oct 31, 1961|
|Priority date||Oct 31, 1961|
|Publication number||US 3283028 A, US 3283028A, US-A-3283028, US3283028 A, US3283028A|
|Inventors||Eric V Bergstrom, John G Mitchell|
|Original Assignee||Mobil Oil Corp|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (11), Referenced by (7), Classifications (37)|
|External Links: USPTO, USPTO Assignment, Espacenet|
NOV- 1, 1966 E. v. BERGsTRoM ETAL. 3,283,028
THERMAL CONVERSION PROCESS AND APPARATUS THEREFOR Filed Oct. 31, 1951 2 Sheets-Sheet 1 INVENTORS .EH/c l/ @mesmo/w a/oH/v G. M/TCHELL ATTORNEY NOV- 1, 1966 E. v. BERGsTRoM ETAL 3,283,028
vTHERMAL CONVERSION PROCESS AND APPARATUS THEREFOR Filed oct. 31,1961
2 Sheets-Sheet 2 F/GZ 1N VEN TOR E/WC V BERGSTROM JOHN G. M/TCHEZTL @gi/M mw ATTORNEY United States Patent O 3,283,028 THERMAL CONVERSION PROCESS AND APPARATUS THEREFOR Eric V. Bergstrom, Byrarn, Conn., and .lohn G. Mitchell, Larehmont, N.Y., assignors to Mobil Oil Corporation, a corporation of New York Filed Get. 31, 1961, Ser. No. 149,069 16 Claims. (Ci. 260-683) he present invention relates to an improved process for carrying out thermal conversion reactions and .apparatus useful therefor. More particularly, the invention relates to a process for carrying out thermal conversion reactions requiring a relatively high temperature and apparatus adapted to` carry out such thermal conversions.
In reference to the process embodied by this invention, it is mainly directed to thermal conversion reactions for materials requiring for thermal conversion a reaction temperature in the range of from about 1200 to about 4000 F. and heat of reaction of from about 2000 to about 12,- 000 B.t.u. per pound. Although the invention may be used with advantages for carrying out many different types of reactions requiring such temperatures and heat of reaction to effect desired conversions, it is particularly useful -with respect to production of unsaturated hydrocarbons by pyrolysis of more saturated hydrocarbons. Thus, reactions embodied by the present invention include production of ethylene and/ or acetylene by prolysis of propane, butadiene by pyrolysis of propane or naphthas, methylacetylene and propadiene by pyrolysis of isobutylene, ketene from acetone, isoprene from branched hexenes, and other pyrolysis reactions including, in general, pyrolysis `of appropriate hydrocarbons to produce mixtures of more unsaturated hydrocarbons, e.g., mixtures of ethylene and acetylene with temperatures of reaction being one of the main factors as to which product predominates in the reaction product mixture. When, for example, it is desired to produce acetylene as the major product, methane and/or natural gas may be used as the charge stock with pyrolysis being carried out at, preferably, about 2400-2800 F., whereas propane and light naphthas may and are preferably pyrolyzed at about 1500 F. or more, c g., up to 2000 F., for production of ethylene as the major product. Still other reactions embodied by this invention include production of carbon and hydrogen from methane, hydrogen cyanide by reacting methane with ammonia, carbon disulfide by reaction of sulfur with methane, acrylonitrile by reaction of ammonia with propylene, and others.
Typical of several reactions for which the present invention is suitable and the reaction temperatures and heat of reaction suitable therefor are the following:
Heat of Reactant Predominant con- Reaction reaction version product temp. F.) (B.t.u./1b.) of reactant Propane- 2, 400 4, OGG-4, 200 D 1,600 l, 900-2, 200 Ethane-- 1, TCO l, 80G-2, 000 Ethyl l, t100-2, 000 1,400-1, 700 l, 500, 1, E 1, 80G-2, 200 2, 100 3, 200-4, 000
Patented Nov. l, 1966 given quantity of defined reactant at conversion temperatures lower than heretofore employed by certain Vother processes; and, in many cases, illustrative of -which is the production of unsaturated hydrocarbons by pyrolysis of more saturated hydrocarbons, the obtainment of desired conversion with minimized production of dry gas, thereby reducing gas plant requirements, and minimized formation of coke and polymeric substances. Still other objects, features and advantages of the present invention will be apparent to those skilled in the -art from the following detailed description thereof.
In accordance with the thermal conversion process embodied herein, reactions requiring a temperature and heat of reaction as aforediscussed are carried out by passing the reactant (or reactants, as the case may be), preferably preheated but to an elevated temperature below conversion temperature, through a reaction zone which, by internal surfaces defining said zone, confines the reactant in the conversion zone to a stream having in cross-section an axis averaging not more than about 0.1 inch and preferably substantially less, said reactant being maintained in said reaction zone for from about 0.0001 to about 0.01 (and preferably from about 0.001 to about 0.01) seconds while, by indirect heating, a reaction ternperature of from about 1200 to about 4000" F. and a 'heat of reaction of from about 2000 to about 12,000 B.t.u./lb. of reactant is maintained in the reaction zone by supply to said zone of a heat ux in the range of from about 20,000 to about 200,000 B.t.u./hr./sq. ft. of internal surface of said reaction zone through which heat is supplied and which is at least one of the surfaces confining said stream to said dimension. By use of such a process, in which the reactant passing through the reaction zone picks up heat by convection, it has been found that the required heat of reaction can be provided through a minimized area of heat transfer surface thereby markedly reducing residence time requirements whereby not only are the aforesaid advantages obtained but, of considerable importance, undesirable and objectionable deposition of solids (e.g., coke) on the internal surfaces of the conversion zone is obviated or substantially minimized, thereby enabling carrying out the desired conversion reaction for extended periods of time with minimized requirements for frequent s-hutdowns due to plugging or stoppage of reactant ow through the conversion zone. In carrying out the aforedefined process, it has been found that the reactant can be passed through the reaction zone at such relatively high linear velocity, and exposed to the reaction temperature for such short periods of time, that any coke that may be formed is carried out of the reactor rather than adhering to wall surfaces of the reaction zone.
ln one embodiment, the invention is practiced by use of a reaction zone substantially rectangular in cross section having a charge inlet at one end portion and a product discharge outlet `at the opposite end portion and which reaction zone, in cross section, has its smallest axis defined by wall surfaces spaced apart by an average distance of notmore than about 0.1 inch and through at least one of which Wall surfaces heat is indirectly supplied to the reaction zone to the extent of the aforesaid 20,000 to 200,000 B.t.u./hr./ sq. ft. of internal surface area through which heat is supplied. For such an embodiment and other embodiments described herein as Well as in general aspects, the method of this invention is practiced with use of a reaction zone that in length is .at least about thirty times the aforesaid dimension of not more than about 0.1 inch.
In another embodiment, the reaction zone is of annular configuration such as may be provided by means of two coaxially disposed, concentric cylinders with one being of smaller outside diameter than the inner diameter of the other shell and of such dimensions whereby an annulus averaging not more than vabout 0.1 inch is provided with the annulus being in open communication at one end portion with an inlet means for charging reactant and at the opposite end portion with a discharge outlet for discharging reaction product, and to Whi'ch lannulus heat ux to the aforesaid extent is supplied yby indirect transfer through the walls of at least one of said cylinders. Although still other congurati-ons may be used, as long as the reaction zone for practice of the method embodied herein confines the reactant to a stream having, in cross section, an =axis averaging not more than about 0.1 inch, and preferably substantially less such as on the order of from about 0.008 to about 0.07 inch, a reaction zone cornprising an annulus formed by concentric, coaxially disposed substantially cylindrical walls is preferred.
In a particularly preferred embodiment, the invention is carried out in a unitary apparatus comprising an elongated annular zone ancl which annular zone is used as a confined path for sequential preheating of charge material, conversion thereof, and'quenching of the reaction product; 4and particularly in connection with such an em- Ibodiment, a novel apparatus, as discussed more fully hereinafter in describing the apparatus of FIG. I, whereby a combustible gas mixture is utilized to provide the required Iheat ux into the conversion portion of the annulus by indirect heat exchange, an oxidizing component of the ultimate combustible gas mixture, prior to combustionV and at an inlet temperature substantially lower than fuel gas combustion temperature, is used to quench the reaction product to an appropriate quench temperature by indirect heat exchange in the quench portion of the annulus whereby the oxidizing component is raised to combustion temy perature, and the combustible gas mixture following combustion and heat release to the conversion zone is used to preheat the charge material, passed into the preheat portion of the annulus, by indirect heat exchange wherein the completely combusted gas mixture gives up sensible heat to preheat the charge.
Regarding the means for supplying the required heat ux, by heat transfer through at least one wall defining the conversion zone, as aforediscussed, there may be used any of several types of heat supply means depending on suitability for use in the particular apparatus in which the desired reaction is carried out. Thus, embodied for use in practice of this invention are furnace burning fuels (liquid or gaseous fuels in air, oxygen, etc.) to supply the required heat by convection and/or radiation, induction coils, electrical resistance heaters, nuclear reactors, and others.
In carrying out the reactions embodied herein and illustrated by reactions involving pyrolysis of hydrocarbons, a carrier gas is, in some instances, desirably used with the charge materials. Thus, a gas such as steam is, in some instances, desirably used as its presence may aid in maintaining high velocities, reduce coke formations that may tend to deposit on interior walls of the reaction zone Iand reduce the partial pressures of the hydrocarbons whereby yields of desired unsaturated products is maximized. Although steam is a preferred carrier gas Ibecause of removal of coke deposits, if formed in some instances, through Water-gas reaction and its ease of separation from the product, other gases such as hydrogen, nitrogen etc. may be-used to help maintain high velocities and lower the partial pressure of the hydrocarbon charge, but with respect thereto, consideration is given torequirements for separation of such carrier gases from the desired produ'cts of the reaction product mixtures.
In order to further describe the invention, reference is made to the drawings in which there are set forth embodirnents of apparatus suitable for carrying out processes as aforediscussed.
In the drawings, FIG. I is an elevation view, parti-ally in section, of a reactor apparatus adapted for conducting the process of this invention; FIG. II is a perspective View of elements of a reactor suitable for carrying out the process embodied herein; and FIG. III is 'an elevation View, partially in section, of a further embodiment of va reactor, adapted for use in conducting the process embodied herein.
In reference to the apparatus aspects of the present invention, FIGS. II and III illustrate embodiments of apparatus which, when so designed that the reactant introduced into the conversion zone is conned to a steam averaging not more than about 0.1 inch for its smallest axis in cross section, the thermal conversion process ernbodied herein can suitably be carried out. In the case of apparatus as shown in FIG. II, the feed to the reactor is preheated by means separate from the reactor as is also the case for quenching of conversion product exiting-from the reactionzone. Similarly, for the apparatus of FIG. III, the main preheating of the feed material is generally accomplished by .extraneous means as may also -be the case for accomplishing substantial quenching of the conversion product. However, in an apparatus illustrated by the embodiment of FIG. I, there is provided an apparatus of unitary type that comprises such a novel combination and arrangement of elements whereby, in a single apparatus, the feedV material is preheated, converted and the converted product is quenched. When so designed that the material to be converted is confined, in the reaction zone of apparatus as shown in FIG. I, to a stream having, in cross-section, a minor axis averaging not more than about 0.1 inch, the .apparatus of FIG. I provides a highly effective means for carrying out the method of this invention at the aforestated short residence times. However, in the novel combination and arrangement of elements as is illustrated by the apparatus of FIG. I, there is provided an apparatus which is adapted for carrying out thermal conversion reactions `of more generic scope than `the method defined hereinbefore for example, and as is apparent from the description of the apparatus of FIG. I set forth hereinafter, the apparatus is highly suitable for carrying out thermal conversions at, for example, longer residence times than aforediscussed and in which case the apparatus of FIG. I can be so designed such that reactant passing into the conversion zone is not confined to a stream having,V in cross section, an axis averaging not more than about 0.1 inch but to a stream that vcan `be of much larger dimension las to such an axis. Thus, by the embodiment of FIG. I, there `is illustrated an apparatus useful for carrying out thermal conversion reactions in more generic manner than the aforesaid deined method and in which more generic aspects, the apparatus of FIG. I provides a unique. combination and arrangement lof elements whereby in a unitary apparatus, a material to be thermally converted can be preheated, converted and quenched under highly eicient thermal conditions. Although in the more detailed description of the apparatus of FIG. I particular emphasis has been made on its use for carrying out thermal conversions under substantially lshortresidence times, it should be apparent that in its adaptability to carrying out of thermal conversionsy in general, the apparatus of FIG. I can be so designed as to confine the reactant stream in the reaction zone to a ditionally, a unitary-'apparatus as set` forth by the embodi. ment of FIG. I provides means, for carrying out thermal.
conversion processes, with materially reduced investment for equipment as it minimizes or obviates the need for separate means for substantial preheating of the reactant, for providing the required conversion temperature, and for quenching the conversion product. Moreover, such an apparatus obviates the need for introduction of quench media into the conversion product which rn-ay not only contaiminate the conversion product but would require extensive and expensive equipment for separation of quench media from the desired conversion product, etc. Such advantages provided by an apparatus as shown in FIG. I result from the hereinafter described combination and arrangements of elements whereby, in a unitary apparatus, the conversion product is quenched by indirect heat exchange with an oxidizing gas whereby the oxidizing gas is raised to combustion temperature, mixture -of the resultant thus-heated oxdizing gas with a fuel gas whereby the mixture undergoes combustion and, by indirect heat exchange, provides the required heat flux for thenial conversion, and sensible heat from the combusted mixture is then used to preheat the charge =by indirect heat exchange.
Referring to the drawings, there is shown in FIG. l a reactor having a vertically elongated substantially cylindrical outer metal shell 1 and, coaxially disposed therewith, a vertically elongated substantially cylindrical metal inner shell 2 with shell 2 having a smaller outside diameter than the inner diameter of shell 1 whereby `an annular space D is provided in between the outside Wall of shell 2 and the inner Wall of shell 1. The outer shell 1 is supported, at its base, by support flange 3 by means of bolts 4 which, when tightened, compress gasket 5 to form a seal between shell 1 and support flange 3, Support flange 3 has, as shown, van appropriate internally threaded opening 6 to .accommodate an externally threaded inlet conduit 7 in open communication with charge inlet plenum 8 formed by support flange 3 and ange 9. Flange 9 also serves to support inner shell 2 at its base with gasket 10 disposed in between ange 9 and the base of shell 2 whereby a seal is formed in between flange 9 and the base of shell 2. By means of internally threaded ring 11, engaging external threads of support member 9, tightening of ring 11 serves to compress gasket 12a .and seal the inlet plenum 8. With flange 9 having a smaller outside diameter than the inner diameter of shell 1 and flange 3, the inlet plenum 8 is in open communication with the annular space D. Flange 9, as shown, has an appropriate central opening providing a gas outlet conduit 13 which, as later discussed, is for discharge of combustion gas from the reactor.
At the top portion of outer shell 1, there is disposed a gasket 14 between the top of shell 1 and flange 15, the latter being bolted to shell 1 by means of bolts 21 whereby gasket 14 is compressed to provide a seal between shell 1 and ange 15. An appropriate internally threaded opening is present in flange 15 to accommodate an externally threaded product discharge conduit 16 in open communication with product discharge plenum 17. Plenum 17, as shown, is provided by the walls of flange 15 and ange 18 that closes the top of the reactor and, being of smaller outside diameter than the inner diameter of shell 1, annular space D is in open communication with plenum 17. To seal plenum 17 and provide for differential thermal expansion, packing gland follower ring 19 compresses packing 20 by means of bolts 29a engaging appropriate threads in flange 15. Thus, material charged via inlet conduit 7 is confined to passage into inlet plenum 8, annular space D, plenum 17 and discharge via product outlet conduit 16.
For the embodiment shown in FIG. 1, the vertical elevation of the reactor is divided into a preheat zone designated as A-A, a conversion zone designated as A-B, a fuel mixing and initial combustion zone designated as B-B, and a reaction product quench zone designated as B'-C. Within the reactor, and for substantially the vertical elevation of the quench section B-C, there is disposed metal shell 25 which is substantially cylindrical and coaxial with metal shell 2. The bottom and top portion of shell 25, at its outer periphery as at 25a and 2517, is of such dimension as to tightly abut the inner wall of shell 2 thereby providing at the top 4and -bottom portion of shell 25 a gas seal with shell 2. Intermediate the sealed top and bottom portion of shell 25, the outside wall of shell 25 is indented whereby a confined annular space E is provided between shell 2 and shell 25 which, as shown, is provided with an inlet orifice 26 (or a plurality thereof, not shown) and a gas outlet orifice 27 (or a plurality thereof, not shown) at the top and bottom portions respectively, of shell 25. By means of gas inlet orifice 26, the confined annular space E is in open communication with plenum 28, and by means of orifice 27, the annular space E is in open communication with a gas mixing zone M. Thus, an oxidizing gas (e.g., combustion air, the flue gas-air mixture) introduced via conduit 12 is confined to passage in plenum 2S, into annular space E via orifice 26 and out of annular space E via orifice 27 into mixing zone M.
Extending through an appropriate opening at the top of the reactor, i.e., at the top of flange 18, is an externally threaded conduit 30 engaging internal threads in flange 18, said conduit 30 being in turn in open communication with a downwardly extending conduit 31 which, by means of external threads at its bottom portion, engages an internally threaded gas distributor 32 which, by means of welds at 33 is rigidly adhered to shell 25 and seals plenum 28 from mixing zone M. In gas distributor 32, a plurality of orifices 34 are provided whereby a fuel gas introduced via conduit 30 is confined to passage through conduit 31 and orifices 34 into mixing zone M. Orifces 34 are so positioned as to direct the fuel gas exiting therefrom tangentially into the gas exiting from orifice 27 whereby uniform gas mixing occurs in zone M.
For further sealing of plenum 28 from annular zone D and to aid in support of the assembly, a studded ring 35 is bolted by means of bolts 36 to flange 18. Seal gasket 42 is provided for such sealing when compressed by tightening bolts 36.
Also disposed within the reactor is a suitable refractory 40 (e.g., mullite) in the form of a substantially solid cylinder of smaller diameter than the inside diameter of shell 2 and coaxially disposed with shell 2 whereby annular space F is provided between refractory 40 and shell 2. By use of an integral refractory centering plug 36, refractory 40 is maintained in position by an appropriate centering indentation, as by indentation 43 in gas distributor 32. The refractory 40 extends, as shown, upwardly in the reactor to an elevation defining the bottom of gas mixing zone M.
At its bottom portion, refractory 4f) has a centrally disposed centering extension 45 that 1'its into an accommodating indentation 44 of a member 46 having a closed top, and open at the bottom, such as to form plenum 41 in open communication with combustion gas discharge conduit 13. As shown, the outside diameter of member 46 is smaller than the inside diameter of shell 2, whereby, being coaxially disposed with shell 2, an annular space is provided between shell 2 and member 46 and which annular space is a continuation of annular space F. As is further shown, the bottom of member 46 is, at its outer periphery at 46a, of outside diameter such as to abut against the interior wall of shell 2 whereby, in combination with split ring collar 47, ring collar 47 transfers compression caused by tightening bolts 48 to provide a seal via gasket 10, thus sealing plenum 41 from annulus D and plenum 8. Member 46 has an orifice 49 (or a plurality thereof, not shown) providing open communication of annular space F with plenum 41 whereby, a gas mixture from zone M is confined to passage into annular space F and from F to plenum 41 via orifice 49 and out of the reactor via outlet conduit 13.
In the apparatus of FIG. I and the described arrangement and disposition of the components thereof, feed reactant is introduced via conduit 7 into plenum 8 from which it passes into and up through the preheat portion A-A of annular space D, into the conversion portion A-B of annular space D and into the quench portion '-C from which the quenched reaction product passes into plenum 17 and out of the reactor via conduit 16.
An oxidizing medium (e.g., air, flue-gas-air mixture) is introduced via conduit 12 into plenum 28 from which the air passes Via orifice 26 Vinto and then downward through annular space E and, thence, via oriiice 27 into gas mixing zone M. A combustible gas, such as a fuel gas, is introduced via conduit 30 through conduit 31 and orifices 34 into gas mixing zone M wherein the air from orifice 27 and gas from orifices 34 mix `and undergo initial combustion in the area of M and complete combustion in passing through annular space F whereupon the burned gas mixture enters plenum 41 via orifice 49 and is discharged from the reactor via conduit 13.
As an embodiment for carrying out a process embodied herein by utilizing the apparatus of FIG. I, air is fed via conduit 12 and a fuel gas is fed via conduit 30, at substantially below combustion temperature, and in proportions to provide a suitable combustible mixture. The relatively cool air that passes via orifice 26 into annular space E is heated by abstracting heat passing through shell 2 from the hot reaction product in annulus D as it passes` through quench zone B-C from conversion zone '-B of annulus D, resulting in quenching of reaction product in passing upwardly through the quench zone. The resulting heated air, exited via orifice 27 into mixing zone M mixes therein with the fuel gas exiting via orifices 34. With the temperature of the air exiting via orifice 27 having been raised, by indirect heat exchange via the Wall of shell 2, to a temperature sufficient to initiate combustion of the gas-air mixture, combustion is initiated in the area of M', and the combustion mixture upon entering annular space F undergoes complete combustion therein to supply the required heat ux through shell 2 into the reaction zone of annular space D. During downward passage of the combustion gas through the annular space F, heat isk also given up by indirect heat exchange to the charge passing upwardly through the preheat zone A-A of annulus D, whereupon the completely burned gas mixture passes through orifice 49 into plenum 41 and out of the reactor via conduit 13. Y
In such `an operation, the fuel gas-combustion air mixture is completely burned shortly following entry from y zone M'into annular space FV due to surface combustion; and such an operation is carried out using excess air or air-flue gas mixture to control the peak combustion temperature and provide sensible heat exchange balance between the reaction product and air or air-flue gas in the quench section of the reactor, and between the combustion gas mixture and the charge material in the preheat zone.
In a speciic embodiment, untilizing an apparatus as shown in FIG. I for thermal conversion of a light naphtha to a reaction product mixture comprising ethylene, the following sets forth details of a suitable embodiment of such an apparatus and suitable conditions for carrying out such a conversion therewith.
Re actor Vertical height of preheat zone A-A=l% Vertical height of conversion zone A-B=12"4 Vertical 1height of quench zone B'-C=8 Vertical height of mixing zone B-B=21/2" Width of annulus D: 0.0l9-0.031 inch Width of annulus E=0.036-0.048 inch Width of annulus F=0.064-0.l05 inch Thickness of shells 1 and 2=1i inch Outside diameter of shell 1:81/8 inches Materials of construction:
Refractory 40=mullite; expansion coefiicients at 100- 1000 F.=1.8 l06 in./in. F.; at 100-2500" F. =3.4 106 in./in. F.
8 Shell 1 and shell 2=alloy HI; (high chrime-nickel alloy) expansion coeticients at 10G-1000" F.=9.9 l0-6 and at 10U-2000 F.=10.8 X-i in./in. F.
Via condruit 7=97.5 lbs./hr. (naphtha of 280 F. end
point and 20 wt. percent steam) at 400 F. Via conduit 12:283 lbs/hr. at 100 F. of air-uegas mixture (vol. ratio of 1:1) Via conduit 30:7.3 lbs/hr. of fuel gas at 100 F.
Gas temperatures in reactor:
In preheat zone of annulus D at A==400 F. at A- 1300"` F. In conversion zone of annulus D at A=1300 F. at B=1700 F. In quench zone of annulus D at B=1700 F. at C=900 F. In annulus F and annulus E- at A=.1000 F. at A=1770 F. at B=2800 F. at B=900 F. at C= F.
In annulus D at A=66 ft./sec., at A=118 ft./sec. at B-B'=326 ft./sec. at C=193 ft./sec. In annulus F Iand E- at A=282 ft./sec. at A'=278 ft./sec. at B=320 ft./sec. at B=296 ft./sec. at C=l53 ft./sec. Heat linxy into annulus D by indirect heating `through shell 2- at A 265,000 B.t.u./hr./ sq. ft. at A 22,500 B.t.u./hr./ sq. ft. at B 67,000 B.t.u./hr./sq. ft. at B 52,000 B.t.u./hr./sq. ft. at C 37,500 B.t.u./hr./sq. ft.
Residence time in conversion zone.A'-B of annulus D=0.0045 sec. Product discharge via conduit 16=97.5 lbs/hour at 900 F.; total conversion of 93%, about 43% ethylene. Combustion gas discharge via conduit 13=290.3 lbs/hour at 1000 F.
In another embodiment, there is shown in perspective in FIG. II a reactor comprising a rectangular Vmetal plate 50, beveled at the edges asshown at 51,`and a corresponding metal plate 52, also beveled at its edges as shown at 53 such that, by bringing the two metal plates together and welding the plates together at the bevels, there is formed a reactor having a reaction zone 54 in the form of' a slot provided in plate 52 in open communication with an inlet 55 for charging material to be converted into reaction zone 54 and in open communication with an outlet 56 for discharge of conversion product from reaction zone 54. By use of appropriate means, such as a conduit (not shown), inlet means 55 is connected to a source of charge material and, similarly, outlet means 56 is appropriately connected to a conduit or other suitable means for passing discharged product from outlet 56 to storage or to suitable means for quenching the discharged product. In such an embodiment, and for which the required heat ux into reaction zone 54 is suitably provided by use of an induction coil to heat plates 50 and 52, the reaction zone 54 is restricted to a dimension of not more than about 0.1 inch (average) between plates 50 and S2.
In operation, and using an apparatus as shown in FIG. Il of the following size and dimensions, the following Table I sets forth data obtained from several runs, using various types of hydrocarbon charge stocks and the product yields under the conditions set forth in the table.
Size of plates 50 and 52=3% x 2 X 3A Size of inlet S and outlet 56=% slot Reaction zone 54=overall length, 21A", maximum width, 1"; average depth, 0.01.
Material of construction=3l0 stainless or graphite.
For the runs for which data are set forth in Table I, a graphite reactor was used for runs carried out at temperatures above 2000 F. and a stainless steel reactor for the other runs. The runs were carried out with the feed set forth for each run with the exception of the last run in which the charge was 280 F. end point naphtha an inside diameter of one-half inch and about thirtytwo inches long; and plug 61 a refractory material or a metal (e.g. high chrome-nichel alloy) of such dimensions that the annular space between shell 60 and plug 61 is about 0.025 inch. With the induction coil 72 being of suiicient capacity to provide the required heat ux into the annular space by indirect heat exchange While maintaining the reaction zone of the annular space at about 1700 F., a charge (at 400 F.) of 5.1 lbs. of naphtha and 1.3 lbs. per hour of steam is fed via inlet conduit 65 and in passing through the annular space undergoes further preheat and conversion in passing through the portion of the annular space designated X-X (approximately 13 long in the aforesaid embodiment) and in continuing its passage the conversion product undergoes quenching at the zone of Y-Y (approximately 14") and is discharged from the reactor via outlet conduit 69.
As is apparent from the data set forth hereinbefore, and particularly in Table I, practice of the method of this and steam in a weight ratio of steam to naphtha of 1.411. 2O invention results in markedly high thermal conversions TABLE 1 Temp. Heat ux, Products (weight percent, discharged via outlet 56) Feed Temp. of in re- B.t.u./ft. (Atm.) Total Charge via inlet rate, charge, action 2/hr. 103, Partial converlbs/hr. F. zone, into pressure sion, H2 CH; C2H4 C2H2 03H5 02H5 Cr-l- 04H6 04H6 F. reaction percent zone 54 Propane 0. 8 800 2, 600 205 l. 0 98 6. 1 34 5 45 6 0.4 800 1, 750 100 1. 0 92. 7 3.1 21.4 47. 4 5 10 0. 4 800 2, 000 110 l. 0 98 4.1 29. 8 43. 6 11 0 2 Methane 0. 3 1, 100 3, 050 180 1. 0 85 46 54 Ethane 0. 66 800 2, 170 54 1. 0 99 12. 6 22. 2 40. 4 2l 0, 7 0. 66 800 2, 000 40 1. 0 97 6. 5 l0. 6 64. 0 6. 2 1. 2 Ethylene 2 0. 6 800 1, 870 40 l. 0 l5. 5 1. 9 15 46 7. 5 Lt. NaphthzL-. 0.8 500 1, 550 54 1. 0 84 1. 2 11. 2 36 0.7 15.8 L10-280 F 0.5 800 2, 050 50 1. 0 92 5. 9 24. 2 33 26 1. 9 0.5 800 2, 150 50 l. 0 93 9. 7 25. 0 16. 6 41 l. 1 Lt. Naphtha. 3 0. 5 500 1, 750 75 0. 2 91 3. 5 13. 3 4l. 7 3. 1 11. 7
1 Coke. 2 Ethylene recycled to extinction. 3 Naphtha.
4 Includes 9% Ca-land 6% carbon as COrCOg.
In FIG. III of the drawings, there is shown an embodiment of an induction heated annular reactor in which cylindrical metal outer shell 60 is coaxially disposed with a cylindrical plug 61 of smaller outside diameter than the inside diameter of shell 60 and plug 61 whereby there is provided an annular space in between shell 60, such an annular space having an appropriate dimension averaging not more than about 0.1 inch as the distance between the inner wall of shell 60 and the outer wall of plug 61. By means of internal threads, a closure cap 62 engages external threads of shell 60 at threads 63 such as to provide an inlet plenum 64 into which feed to the reactor is charged via inlet conduit 65. At the opposite end portion of shell 60, a closure cap 66, internally threaded, engages external threads 67 of shell 60 such as to provide a product discharge plenum 68 from which conversion products pass out of the reactor via discharge conduit 69. To position, and maintain in position, plug 61 with respect to shell 66, several slot pin spacers 70 and spotwelds 71 are disposed asshown. Appropriately disposed, as a means for providing required heat flux into the conversion zone ofthe annular space between shell 60 and plug 61, is an induction coil 72.
In operation, using the apparatus of FIG. III, the charge material to be converted is fed, preferably preheated, through inlet conduit into plenum 64 from which the charge material is confined to passage through the annular space between shell 60 and plug 61, and then into product plenum 68 and out of the reactor through discharge conduit 69. In an embodiment, and using such an apparatus for thermal conversion of a naphtha to a mixture containing ethylene as the predominant component, shell 60 can be a metal tube (eg. high chromenickel alloy) having an outside diameter of one inch,
of feed stocks, such as saturated hydrocarbons, to produce mixtures containing a relatively large amount of a desired unsaturated compound, depending on the particular conditions employed for directing the conversion to production of the desired compound. Thus, as exemplified by the thermal conversion of propane, total conversions of over can be obtained with, depending on the conditions used in practice of this invention, ields of as high as 45 wt. percent of acetylene, or as high as 47.4 wt. percent of ethylene, or a total as high as 54% as the sum of ethylene and acetylene. Similarly, from ethane, total conversions on the order of 97 and 99% are obtained, as shown in Table I, with wt. percent yields of ethylene as high as 40.4 and 64.0 and, in the case of the 40.4 yield of ethylene, the additional yield of as much as 2l wt. percent of acetylene.
An important aspect of the present invention is that, by practice thereof as aforediscussed and illustrated by thermal conversion of light naphtha for maximum production of ethylene as the most desired product, the present invention can be carried out not only to provide a high conversion to olens but, at the substantially high conversions (eg. 50 wt. percent or more) to total olens, the wt. percent converted to the most desired product (c g. ethylene) can be as much as about 34% when the total conversion to oletins is on the order of about 52%, and the substantially high relative proportion of ethylene to total olefins is obtained even as the total conversion to olens increases to values much higher than about 50 wt. percent. Such a relatively high yield of desired olefin (e.g. ethylene) at exceptionally high values of Wt. percent conversion to total oleiins by a thermal conversion process, as embodied herein, is a marked improvement over certain other known processes for thermal conversion of, for example, saturated hydrocarbons to unsaturated hydrocarbons and which, illustrated by desired production of ethylene from light naphtha, generally provide a reduced proportional yield of ethylene based on total yield of olefins as the total olefin yield increases and, particularly, when the total olefin yield amounts to more than 40 or 50 wt. percent (based on the charge).
Of such other known processes are those of the steam coil type, moving bed converters, (c g. pebble heaters), partial combustion processes, inert uidized bed methods, and others.
Although, in the foregoing description of the invention, and the embodiments used for purposes of illustration and not limitation, certain conditions have been set forth for carrying out the invention, the following tabulation sets forth `a correlation of several conditions that may be used, such as for conversion of more saturated hydrocarbons to more unsaturated hydrocarbons, within the scope of this invention. In such a tabulation, the values shown in the column under I apply for extremely high temperature reactionsV and those un-der II for reactions requiring temperatures on the low side of the temperature range of reactions 4to which this invention is directed. As for reactions requiring temperatures over about 1200" F. and below 4000 F., appropriate values intermediate the ranges shown for each of the conditions set forth in the tabulation can be used.
Residence time in conversion zone (seconds) 01 200, 000 to 20, 000
Heat flux into conversion zone 1 B.t.u./hr./t't.2 of internal surface through which heat is passed.
In the foregoing description of the invention, and in the embodiment vdescribed in connection with the apparatus of FIG. I, the quenching of the conversion product is carried out in the un-itary apparatus by indirect heat exchange with the oxidizing gas (eg. air). In the embodiment describe-d in connection with the Iapparatus of FIG. lil, the quenching can be either fully or partially effected in the annulus,-subsequent to the conversion zone portion thereof, through which the reaction product passes prior to discharge from the reactor and, in such an instance as well as in other embodiments wherein the conversion reaction is carried out as embodied herein, the reaction product can be subjected to quenching by other methods suitable for effecting prompt quenching `by reduction of the product to a temperature at which substantial reaction of components of the product mixture is minimized or completely inhibited. Thus, and illustrated by embodiments utilizing apparatus as disclosed by FIGS. II and III, such quenching can be carried out by recycling product mixture at a substantially lower temperature to the product mixture exiting from the reactor; by use of conventional Waterspray methods, oil quench methods, cooling coils, and others.
In reference to the apparatus aspects of this invention, the materials of construction used therefor, and particularly for structures defining the reaction zone, rthe materials of construction should possess, for the particular ternperature and conversion atmosphere to which they are exposed, a suitable combina-tion of high dimensional stability, expansion coefiicients and thermal conductivity. Other than materials hereiubefore disclosed in describing embodimentsfof apparatus suitable for practiceof this invention, and depending on the particular process to be carried out in the apparatus, materials such as graphite, fused alumina, graphite coated with metals (c g. silicon, tantalum, zirconium, titanium, tungsten, hafnium, molybdenum), cermets, and others may be used.
The conversion process embodied herein can be carried out over a rather wide range of pressure (partial) and, although it is not intended to limit the process with respect 12 thereto, it can `be carried out at sub-atmospheric to` about 70 p.s.i.g.
Although the present invention has been described with particular embodiments, it isto be understood that modifications and variations may be resorted to, without departing from the spirit and. scope `of this invention,` as those skilled in the artwill readily understand. Such Variations and modifiications are considered to be Within the purview and scope of the appended claims. Thus, as embodiments, reactors and the process of `this invention inclu-de use of a plurality of reactors in assemblies such that individual reactors can be put on or taken off stream as desired for servicing, repair, etc.
What is claimed is: p
1. A method for effecting relatively high temperature thermal reactions which comprises passing a thermallyconvertible reactant into a preheat zone of a continuous confined path comprising successively Aa. preheat zone, a conversion zone and a `quench zone and in which path the reactant is preheated -in the preheat zone to an elevated temperature but below thermal conversion temperature, the thus preheated reactant passes into the conversion zone wherein it is thermally converted and the resulting conversion product passes into the quench zone wherein it is quenched to a temperature sufiicient to prevent substantial further reaction of the conversion product, said quenching of the conversion product in the quenching zone, conversion of the preheated -reactant in the conversion zone andpreheating -of the .reactant in the preheat zone being effected by passing an oxidizing gas lat a temperature substantially lower than quench temperature into indirect heat exchange with said quench zone to quench conversion product passing into said zone and to raise the temperature of the oxidizing gas .to a temperature that supports combustion of a mixture of said oxidizing gas with a combustible fuel, .mixing a combustible fuelwith said oxidizing gas raised to said combustion temperature whereby the mixture undergoes combustion and by indirect heat exchange with the conversion zone the 'mixture under combustion supplies the necessary heat flux to the conversion zone, land followingvsaid indirect heat exchange with the conversion zone, passing the combusted mixture into indirect heat exchange with the preheat zone whereby sensible heat of the combusted mixture preheats `the reactant in the preheat zone.
2. A method, as defined in claim 1, whe-rein the oxi` dizing gas is air and the combustible fuel is a fuel gas.
3. A method, asdefined in claim V2, wherein the reactant is a hydrocarbon that is gaseous at the conversion temperature and is thermally convertible to a more unsatu rated hydrocarbon.
4. A method, as defined in claim 1, wherein lthe reactant is a hydrocarbon that is gaseous atv fromabofut 1200 to about 4000 F.
5. A method, as defined in claim 4, fwherein the hydrocarbon is pyrolyzed to a product mixture 4containing a hydrocarbon more unsaturatedthan the reactant.
6. A method, as defined in claim 5, wherein the reactant is from the group consisting of methaue,.ethane, propane, ethylene and naphtha.
7. AV method, as defined in claim 1,-.wherein the reactant passing through the conversion zone' is confined to a stream having in cross section a minor axis of from about 0.008 to about 0.07 inch.
8. A method, as'defined in claim 1, in which the reactant passing through the conversion zone is confined to astream having a minor axis averaging not more than labout 0.1 inch.
9. A method, as defined in claim 8, wherein the conversion zone, in the direction of reactant flow therethrough, is at least thirty times said axis averaging not more than about 0.1 inch.
10. A method, as defined in claim 1, wherein the reactant requires for thermal conversion a temperature in the range of from about 1200 to about 4000 F. and a heat of reaction of from about 2000 to about 12,000 B.t.u./lb. of reactant, the reactant is maintained in the conversion zone for from about 0.0001 to about 0.01 second While the temperature in the conversion zone is maintained at from about 1200 to about 4000 F., and the heat of reaction of from about 2000 to about 12,000 B.t.u./lb. of reactant is maintained in the conversion zone by supply thereto of a heat flux of from about 20,000 to about 200,000 B.t.u./hr./ sq. ft. of internal surface of said conversion zone through which heat is supplied by the mixture under combustion.
11. A method, as defined in claim 1, wherein the conversion zone confines the reactant to an annular stream.
12. A method, as defined in claim 1, wherein the reactant is a hydrocarbon that is pyrolyze-d in the conversion zone to a less saturated hydrocarbon conversion product, the oxidizing gas is air, and the combustible fuel is a fuel gas.
13. An apparatus, adapted for carrying out relatively high temperature thermal reactions, comprising an elongated confined annulus having an inlet means at one end portion adapted to pass reactant into a preheat chamber in said annulus and an outlet means at the opposite end portion for discharge of reaction product from a quench chamber in said annulus, said annulus being characterized by comprising successively and in open communication a preheat chamber, a conversion chamber and a quench chamber with the conversion chamber having internal wall surfaces adapted to confine -reactant passed from the preheat chamber into the conversion chamber to a stream which, in cross-section, has a minor axis averaging not more than about 0.1 inch, means adapted for passing an oxidizing gas into indirect heat exchange with the quench chamber whereby to abstract heat from the reaction product passed from the conversion chamber into the quench chamber and the oxidizing gas is raised to a temperature that supports combustion with a combustible fuel, mixing means for mixing said oxidizing gas Vat combustion temperature with a combustible fuel whereby the resulting mixture undergoes combustion, and means for passage of the mixture under combustion into indirect heat exchange with the conversion chamber to provide the necessary heat flux in said conversion chamber and for passage of the resulting combusted mixture into direct heat exchange with the preheat chamber whereby sensible heat of the combusted mixture preheats reactant passed into the preheat chamber of said chamber.
14. An apparatus, adapted for carrying out relatively high temperature thermal reactions, comprising a vertically elongated confined annulus defined by coaxially and concentrically disposed shells of material adapted to withstand a temperature in the range of from about 1200 to about 4000 F. with one shell having an outside diameter smaller than the inside diameter of the other shell such that the distance between the inside wall of the shell of said larger inside diameter and the adjacent wall of the shell of said smaller outside diameter averages not moreV quench chamber, means for passing an oxidizing gas into indirect heat exchange with said quench chamber, mixing means inside of said shell of smaller -outside diameter for mixing a fuel gas with said oxidizing gas following said indirect heat exchange of said oxidizing gas with the quench chamber, and means adapted for directing passage of the resulting combustible mixture while under combustion into indirect head exchange with said conversion chamber and for `directing passage of the combusted mixture, following vsaid heat exchange with the conversion chamber, into indirect heat exchange with the preheat chamber whereby sensible heat from the combusted mixture preheats reactant passed into said preheat chamber.
1S. An apparatus, adapted for carrying out relatively high temperature thermal reactions, comprising an elongated confined annulus comprising successively and in open communicaton 4a preheat chamber, a conversion chamber, and a quench chamber, inlet means for passing a thermally-convertible reactant into the preheat chamber and outlet means at the substantially opposite end portion of said annulus for discharge of quenched conversion product from the quench chamber, means `adapted for passing 4an oxidizing gas into indirect -heat exchange relationship with the quench chamber, means for mixing a combustible fuel with said oxidizing gas following said indirect heat exchange with said quench chamber, and means to direct the mixture of said oxidizing gas and fuel while under combustion into indirect heat exch-ange with the conversion chamber and, following said heat exchange with the conversion, to direct passage of the combusted mixture into indirect heat exchange with the preheat chamber.
16. An apparatus, as defined in claim 15, wherein the elongated confined annulus is defined by coaxially and concentrically disposed cylindrical members, one of which has an outside diameter smaller than the inside diameter of the other member such as to provide said annulus comprising successively and in open communication a preheat chamber, a conversion chamber and a quench chamber, said means for mixing a combustible fuel with the oxidizing gas being disposed inside of the cylindrical member of smaller outside diameter.
References Cited by the Examiner UNITED STATES PATENTS 1,677,363 7/ 1928 Olivier 260-683 2,283,643 5/1942 Nagel 260-683 2,529,598 ll/1950 Deanesly 260--679 2,543,743 2/1951 Evans 260-683 X 2,644,744 7/ 1953 Hartwig et al. 260-683 2,706,210 4/ 1955 H-arris 260-683 2,786,877 3/1957 King 260-683 2,845,335 7/1958 Hasche 260-683 X 2,868,856 l/l959 Hale et al. 260-679 2,904,502 9/1959 Shapleigh 260-683 X FOREIGN PATENTS 775,666 5/1957 Great Britain.
DELBERT E. GANTZ, Primary Examiner.
ALPHONSO D. SULLIVAN, Examiner.
C. E. SPRESSER, Assistant Examiner.
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US1677363 *||Jun 3, 1926||Jul 17, 1928||Le Petrole Synthetique Sa||Process of treating methane gas|
|US2283643 *||Sep 10, 1938||May 19, 1942||Nagel Theodore||Making gas from oil|
|US2529598 *||Aug 30, 1949||Nov 14, 1950||Universal Oil Prod Co||Reactor for high-temperature cracking|
|US2543743 *||Aug 22, 1947||Feb 27, 1951||Socony Vacuum Oil Co Inc||Method and apparatus for hightemperature hydrocarbon conversions|
|US2644744 *||Feb 26, 1951||Jul 7, 1953||Universal Oil Prod Co||Reactor for high-temperature cracking|
|US2706210 *||Dec 5, 1950||Apr 12, 1955||Wulff Process Company||Process suitable for converting primary hydrocarbons to secondary hydrocarbons|
|US2786877 *||Mar 9, 1953||Mar 26, 1957||Secr Defence Brit||Method and apparatus for carrying out thermal decompositions|
|US2845335 *||Mar 20, 1952||Jul 29, 1958||Koppers Co Inc||Regenerative processes and apparatus|
|US2868856 *||Jun 21, 1955||Jan 13, 1959||Union Carbide Corp||Process and apparatus for partial oxidation of hydrocarbons|
|US2904502 *||Feb 19, 1954||Sep 15, 1959||Hercules Powder Co Ltd||Method of cracking hydrocarbons|
|GB775666A *||Title not available|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US3431082 *||Jul 12, 1965||Mar 4, 1969||Battelle Development Corp||Tube furnace provided with filling bodies|
|US3523759 *||Oct 16, 1967||Aug 11, 1970||Phillips Petroleum Co||Apparatus for producing carbon black|
|US4321130 *||Dec 5, 1979||Mar 23, 1982||Exxon Research & Engineering Co.||Thermal conversion of hydrocarbons with low energy air preheater|
|US6130260 *||Nov 25, 1998||Oct 10, 2000||The Texas A&M University Systems||Method for converting natural gas to liquid hydrocarbons|
|US6602920||Mar 9, 2001||Aug 5, 2003||The Texas A&M University System||Method for converting natural gas to liquid hydrocarbons|
|US7119240||Jul 1, 2003||Oct 10, 2006||The Texas A&M University System||Method for converting natural gas to olefins|
|US20040002553 *||Jul 1, 2003||Jan 1, 2004||The Texas A&M University System||Method for converting natural gas to olefins|
|U.S. Classification||585/634, 585/922, 585/602, 585/633, 585/910, 585/539, 585/924, 585/535, 585/899, 422/201|
|International Classification||B01J12/00, C07C11/02, C01C3/02, B01J19/00, B01J10/02, C01B31/26, C07C4/04, C07C2/76|
|Cooperative Classification||C07C4/04, C07C253/00, C01B31/26, C01C3/0225, C07C2/76, C01C3/0212, C10G9/00, B01J10/02, C10G9/14, Y10S585/91, Y10S585/922, Y10S585/924|
|European Classification||C01B31/26, C07C253/00, C01C3/02D1D2, C01C3/02D1, B01J10/02, C07C4/04, C07C2/76|

domain: chemistry


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domain: artistic


Multi-faceted Kiski Area freshman shows big-play prowess
As a freshman, Justice Evans plays key roles for Kiski Area as the team's starter at cornerback, kick returner and punt returner, as well as one of the top running backs.
The special teams work sparked the Cavaliers to a Quad East victory Friday night.
Evans set up two touchdowns with long punt returns and scored a touchdown himself on a 2-yard run, helping Kiski Area (3-3, 3-2) snap a three-game losing streak with a 24-7 victory over Norwin at Norwin Knights Stadium.
“He has a lot of years to play for Kiski, and he has a lot of special gifts,” coach Dave Heavner said. “We actually put pressure on him to make plays, and every time we ask him to do something, he certainly comes up with big plays.”
Evans' first big play came on the final snap of the first quarter, with the Cavaliers and Knights locked in a scoreless tie. He fielded a Logan Deri punt on his own 35-yard line, picked up a big block near midfield and raced down the sideline before getting knocked out at the Norwin 2.
Four plays later, Chad Kuhn snuck into the end zone from 1 yard out to put Kiski on the board.
A second long punt return, this one covering 20 yards, set up Patrick Turner's 26-yard touchdown run in the third quarter, and Evans capped off the scoring himself with a 2-yard run in the third frame.
“He certainly has a full load on his shoulder, and he produces every single week,” Heavner said. “It's been like that since day one.”
While Evans made big plays on special teams, a team effort offensively and defensively helped Kiski Area earn the victory.
Running back Lincoln Clayton exited the game in the first quarter, but Kuhn, Evans and Turner combined to run for nearly 250 yards and three touchdowns in his place.
Defensively, the Cavaliers shut Norwin out in the second half and sacked quarterback Nick Amendola five times. In its previous three games, Kiski Area allowed 126 points — with the biggest blemish a 56-28 loss to Pine-Richland last week.
“Our defense has been pretty good all year, and we wanted to make sure we came out here and got back to basics,” Heavner said.
Doug Gulasy is a staff writer for Trib Total Media. Reach him at email@example.com.


text:
It might seem strange to meet a guy in a laundromat, but that was where I met Henry.
“Do you know how to operate the washing machine? Sorry, this is new to me,” he said while helplessly carrying an IKEA bag stuffed with bedsheets, pillowcases, and floral cushion covers.
After he separated the whites and colours, we chatted about what we do for a living and what we do for fun. It was instant attraction.
“Do you have a girlfriend?” I couldn’t help asking.
At first, he shifted uncomfortably. Then, he confessed that he broke up recently. “It didn’t end very well, but you know how relationships are,” he continued with a forced smile.
After we exchanged phone numbers, our chats turned into hangouts, and hangouts turned into dates. We had the best time together, and I thought we were a pretty good match.
After two months of dating, the first crack of our relationship began.
One morning, I woke up to 16 missed calls from an unknown number. While I was going through my contacts figuring who it was, the unknown number called again.
I picked up, but the person on the other line hung up after I said hello.
It must be those telemarketers again, I thought.
After that, the person called me again and again. I was half-mad at this point because it was too early for prank calls.
I picked up the call again and said, “I’m not interested to buy any insurance, so please stop calling me.”
There was a three-second silence before a voice cracked.
“How about you stop seeing Henry? Then, I’ll stop bothering you,” she hung up.
I was shocked. Who the hell is she? How did she get my number? Why did she mention Henry?
I was feeling confused and nervous at that point and called my boyfriend. He better not cheat on me, I thought.
“I don’t know who you’re talking about,” Henry said. “Are you sure she mentioned my name?”
“Henry, I was certain she did.”
After my boyfriend tried to calm me down, he told me to block her number. “You need to stop her from harassing you, whoever that is.”
After I blocked the number, my phone went silent.
Two days later, it rang again. This time, it was a different phone number. I freaked out because I wasn’t sure who this girl was, and why she would bother me.
Next, a stream of text messages came rushing into my WhatsApp.
You slut, I know you’re reading this. You better reply me.
Stay away from Henry right now!
If you don’t keep away from him, I’ll find you.
Deep down, I was furious. Who was she to call me a slut?
Then, I sent screenshots of her messages to my boyfriend and demanded that he explain the situation to me. Clearly, he was hiding something.
He confessed. “Shit, that’s my ex-girlfriend, Emily.”
Henry and I had a long talk about how to deal with the constant texting and missed calls from Emily. Part of me was angry that I was dragged into this situation. I hate being caught in unnecessary drama.
“You have to fix this, Henry. I can’t keep blocking her phone number like this,” I said.
At that point, she texted me with three different numbers. Her last text message tested my patience.
Bitch, pick up my fucking calls.
I hate being disrespected that way when I didn’t do anything wrong.
“Okay, I’ll go talk to her. For now, just keep ignoring her,” Henry advised.
That same night when I had the talk with Henry, my best friend sent a message.
Cheryl, someone named Emily added me on Twitter and she’s tweeting mean things about you. What’s going on?
I was shocked. I quickly went to Twitter and realised she added all of my friends to her fake profile. Every single one of my friends.
To my horror, she tweeted the same angry messages and every one of my friends was reading it.
Who the fuck does Cheryl think she is for stealing my boyfriend?
Bitch, quit pretending like you’re innocent.
You fucking whore, come out and deal with me in person.
There I was, reading helplessly while Emily was out there writing nasty things about me.
And all Henry wanted me to do was ignore her?
I called and shouted at him for not fixing this situation fast enough.
“How the hell am I supposed to deal with this? She added all of my friends and humiliated me on Twitter! And you’re telling me to not say anything?”
I was at wit’s end. At that point, I was so afraid that she would take the rant to Facebook where my parents and siblings are.
What would my relatives think if they found out about this? What would my parents say if they read a stranger calling me a whore? What am I going to do if that happens?
My friends started texting me personally and asking what the beef was about. That time, all I could say was “Please ignore her. I don’t know who the hell she is.” I even asked my friends to report her on Twitter in hopes of taking down her account.
While dealing with the shame from it all, Henry wasn’t offering the best help. “Cheryl, I did the best I can. I told her to stop disturbing you, but she won’t listen to me!”
My blood boiled and all I could say was, “Just fucking fix this, Henry! I can’t take it anymore!” I knew my reputation was ruined.
I was working in the local cafe that weekend. It was a rainy Sunday afternoon, and the cafe was filled with customers. I manned the counter that day and took drink orders as fast as I can. Dealing with frustrated and impatient customers were the last things I wanted.
After a regular customer paid for his caramel latte, a petite woman walked up to the counter. She had short hair, tanned complexion, and looked visibly upset. I knew I should have cut the conversation short with the previous customer.
“Hi, what would you like to order today?”
“Just a chocolate ice blended.”
“Would you like a small, medium or large?”
“With whipped cream on top?”
“Can I have your name?”
My marker stopped when I tried to spell out her name on the plastic cup. Wait, is she the same Emily who texted and tweeted about me?
My face went pale. She looked right at me and gave me a smirk. I tried my best to compose myself and pretended like I didn’t recognise her. I attempted to scribble her name on the cup, but it became undecipherable.
Fuck, how did she know I work here?
“Got it. That’s RM12.90 please.”
When she walked past me and waited for her drink at the pick-up counter, I panicked. I felt goosebumps everywhere. Is she seriously stalking me at my workplace?
As I took more drink orders from the remaining customers, her sharp and angry gaze didn’t leave me. Her eyes followed my every move. She even chose to sit at the table opposite the counter, attempting to intimidate me.
Once in a while, our gaze met, and I quickly pretended to look away.
Is she planning to cause a scene? Why does she keep staring at me? Is she going to hurt me like she said?
Thankfully, more customers poured in since it rained heavily outside. That left us with little opportunity to talk. I pretended her presence didn’t bother me, and continued taking orders until she left 45 minutes later.
Even in her absence, I still can’t shake the feeling of being watched. What if she’s outside the café, waiting to pounce on me? What if she’s watching me from afar? Was that her sitting on the bench, outside?
When my shift ended, I checked my surroundings and ran to my car before she could notice me.
I knew I couldn’t take it anymore and refuse to live in fear. I called Henry that night and ended our relationship.
Several days after I broke up with Henry, the missed calls and text messages stopped. Despite the silence, I was still afraid that she would show up at the cafe where I worked, but she didn’t.
She finally got what she wanted. A break-up between Henry and I. That was all she wanted, and it sucked to let her win.
If it weren’t for her, Henry and I would still be together. You might think that I should have stuck with him through thick and thin, but I can’t tolerate the humiliation that Emily had caused me.
She embarrassed and insulted me in front of my friends. The fact that she found out about my workplace and stalked me scared the crap out of me.
The relationship simply wasn’t worth it.
Part of me felt sorry for Henry for giving up easily, but I also felt he wasn’t doing enough to amend the situation either. Was it possible that Henry was afraid of her too?
Besides, the last thing I wanted was for my family (the last unaffected party) to get tangled in this unnecessary drama.
What I Learned
While the experience with my partner’s crazy ex-girlfriend wasn’t great, I realised the non-confrontational approach prevented me from worsening the situation. In some ways, Henry was right.
Firstly, remain calm
It’s a tough one to practice, but the last thing I wanted to do was add more fuel to the fire. It was clear that Emily had unresolved issues with Henry. She had to channel her frustration towards someone else, and that person was me.
Thankfully, I had Henry and my best friend to calm me down. Emily however, had to deal with her pent-up frustrations alone.
Having a support system helped me to remain calm and became the bigger person in the situation.
Secondly, ignorance is bliss
To be honest, it wasn’t blissful from my end, but ignoring her did help to defuse the tension.
If I allowed my anger to dictate my response, I would have lashed at her. However, if that happened, it would have opened up a line of communication between Emily and myself. So, nope. Ignorance is better.
Lastly, don’t fight fire with fire
I know the right thing to do is to stand up for myself, but in reality, I’m a non-confrontational person. That’s why I refused to fight fire with fire.
At the same time, I denied her the power to attack me. I pretended like it didn’t bother me, even though it did. Imagine how crazy our first meeting would be if I responded negatively towards her?
While the relationship was good while it lasted, I felt I did the right thing by moving on without Henry. Whatever unresolved issues they had between them, I hope Henry and Emily carried on with their lives peacefully today.
As for me, I’m just glad I never heard from her anymore.
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domain: literature


text:
Bupa Hong Kong, a leading health insurance specialist, has partnered with global health engagement company, Tictrac, to bring Bupa4Life to Hong Kong, a new wellness engagement platform that helps customers understand their health conditions and encourages them to make positive lifestyle changes.
The mental and physical health problems have been exacerbated by Hong Kong’s fast-paced lifestyle, with 20% of the city’s employees working an average of 11 hours a day in 2018, or experiencing a decline in mental health due to COVID-19, with nearly half of Hongkongers noting the effect it is having on them.
Bupa4Life empowers people to take control of their wellbeing. Using Tictrac’s comprehensive engagement platform, it provides Bupa Hong Kong’s corporate customers and individuals with a digital companion that helps them adopt and maintain a healthy lifestyle.
Users will benefit from a range of compelling in-app features that help them to analyse, achieve, assist and award their health and wellbeing needs. To begin, an online health assessment can be completed in just five minutes (Analyse). Users are then encouraged to set action plans and take up tailored monthly challenges to achieve their health goals (Achieve). A daily activity tracker can track their progress. Users will also have access to rich, interactive content which provides daily inspiration, such as health hacks, recipes, and exercise techniques from leading health and wellbeing contributors, and join health events, talks and classes organised by Bupa Hong Kong throughout the year (Assist). A reward programme recognises progress and motivates users to maintain their healthy lifestyle (Award).
Andrew Merrilees, General Manager, Bupa Hong Kong, commented: “After a really tumultuous year, Hongkongers are experiencing greater stress-related health issues. This is why we are stepping up our support to our customers by providing them with the tools they need to improve their health, all in the palm of their hand.
“Tictrac has enabled us to innovate at speed, taking our existing wellness proposition to the next level and providing a complete digital wellness experience. With Bupa4Life, we’re able to connect people with holistic health and wellness support while having fun, anytime, anywhere.”
Martin Blinder, CEO and founder, Tictrac, said: “We are committed to improving the health and wellbeing of communities all around the world. We feel honoured to be partnering with Bupa Hong Kong in providing Bupa4Life to their members, empowering people to lead healthier and happier lives.
“Through our platform, Bupa’s corporate customers can now support their employees in pursuing a healthy work-life balance and encourage them to improve their lifestyle both in and out of work. Individual users will benefit from Bupa Hong Kong’s personalised plans and content to help them become healthier in the long-term.”
Tictrac’s platform has been cleverly designed to seamlessly fit into an individual’s daily lifestyle to deliver lasting behaviour change. It uses behavioural science techniques to identify trigger points where extra motivation may be required, and provides fresh and engaging content to keep users engaged each day. Bupa4Life makes it easy for users to track their activity, whilst supporting and rewarding them with access to tailored health and wellbeing content, products and services, all in one single platform.
Bupa Hong Kong recently launched the ‘Feel Better’ Mental Health Campaign 2020 to make mental health support and services more accessible, enjoyable and sustainable in the city, including the gradual extension of mental health coverage to Bupa policies. The Bupa4Life platform complements the company’s strategy to further support members with their holistic health.

domain: news


Are you tired of using outdated and time-consuming methods for metal engraving? Do you struggle with achieving precision and clarity in your designs? The solution is here: handheld laser etcher for metal.
Say goodbye to the frustration of traditional methods and unlock a new level of creativity with the power of laser technology. Whether you’re a professional jeweler or a DIY enthusiast, a handheld laser etcher for metal will revolutionize how you work and elevate the quality of your projects.
Prepare yourself to tap into your artistic side and discover the limitless potential of laser etching.
Portable Laser Etching Metal
Compared to traditional etching methods, handheld laser etchers for metal offer several advantages. Such as faster etching speeds, greater precision, and the ability to etch complex designs.
However, it’s crucial to consider the limitations and safety precautions when using these devices.
Note: Laser engraving and marking are processes similar to etching a material, but they have some differences.
You can read our article to understand the dissimilarities between Laser Engraving, Etching, and Marking.
Core Features of the Handheld Laser Etcher Machines
Power Output Source
The power output source is a critical feature of portable laser etchers as it determines the intensity and quality of the laser beam. Some models offer the option of using AC or Battery Power, while others may use only one of these power sources.
The operating system and software of portable laser etchers determine their functionality and ease of use. Most models offer intuitive software that enables users to create and edit designs before etching.
Portable laser etchers require a reliable and long-lasting battery, which allows users to utilize them in remote areas or while traveling. Most models come with rechargeable batteries, while some offer swappable battery packs.
The cooling system is an essential feature of portable laser etchers as it prevents the device from overheating during extended use. Models may use air or water cooling systems, with water cooling offering better heat dissipation.
Portable laser etchers require connectivity options to transfer designs from computers or mobile devices, enabling users to work conveniently. Most models offer Wi-Fi or Bluetooth connectivity, while some come with USB or Ethernet ports.
How to Use handheld Laser Etcher for Metal Work?
We have two options to etch metal up to 0.001 inches depth label.
- By melting metal surface to label the design on it.
- Add chemical sprays on metal surfaces, then melt the sprayed surface with a laser etcher machine.
You can use the best sprays from one of these:
|CerMark Ultra Laser Marking Aerosol
|LaserBond Spray 100
|Enduramark For Metals
Types of Handheld Laser Etcher for Metal
The market offers a range of handheld laser etchers for metal from different brands and models. Various applications require specific features and capabilities, which vary among each model.
It’s essential to compare the different models and brands to determine the best one for your needs.
We have identified a few of the best etchers for you to choose from.
Portable Laser Pecker Machines
You have the option of laser pecker machines to etch metals. It comes in various classes. You can go with class 1, 2, and 3 pecker machines.
|450nm NICHIA Diode Laser
|Infrared 1064 nm
|Suit, Basic, Deluxe, Super, mini
|Suit, Deluxe, Basic,
|Click for Amazon
Pecker machines are handheld and can use everywhere. You can even cut metals with these etchers, but the recommendation is to do it multiple passes instead of in one go.
xTool Laser Machines
The xTool Laser Machines company provides a handheld laser etcher for metal. It enables users to etch different types of metals with ease and precision.
These compact, portable, and user-friendly devices make them the best option for small-scale etching projects.
Why Choose Handheld Laser Etcher over Other Etchers?
Small Business Capability
Handheld laser etchers are ideal for small business applications. It is due to their ability to etch complex designs with greater precision and speed comparing traditional etchers.
These are lightweight, making them easy to maneuver and use for extended periods without fatigue.
Traditional etching methods cannot achieve intricate designs on metal surfaces. But these machines enable the marking of such labels with ease.
Handheld laser etchers are designed with ergonomic features such as comfortable grip handles and adjustable settings, making them easy to use and operate for prolonged periods.
Tips To Etch Metals With Handheld Laser Etcher
- Make your safety features as instructed by company manual instructions
- Don’t Put your spray bottles inside the machine
- Sprayed metal must be dry before starting work on it.
- As a beginner, you must create a test project before moving on to the main object to ensure clarity and accuracy.
How to Use the Handheld Laser Etcher for Metal
Step 1: Get Your Design Ready
Before you start using your handheld laser etcher, you need to have a design in mind. It could be a logo, text, or image; that you want to etch onto a piece of metal.
Step 2: Import the Design
To import your design into the laser etcher’s software, you typically need to connect via USB or Bluetooth.
Step 3: Edit the Design
Make some adjustments to get it just right. You can use the laser etcher’s software to resize, rotate, and crop your design.
Step 4: Mark Your Design By Handheld Laser Etcher
You’re ready to start etching your metal. Position the laser etcher over the area you want to Etch and press the button to start the etching process. With a steady hand and some patience, you’ll have a beautifully etched design in no time.
Applications of Handheld Laser Etcher Machines For Metal
You can create intricate designs on metal jewelry pieces using handheld laser etchers.
In industrial manufacturing, people can use them to mark and etch metal parts such as stainless steel, aluminum for identification purposes.
Personalization and customization:
They are great for adding custom designs, logos, or text to metal items such as phone cases, keychains, and trophies.
Conclusion (Handheld Laser Etcher For Metal)
In conclusion, the handheld laser etcher revolutionized metalworkers’ personalization and etch metal items. It offers a new level of flexibility and precision. They offer advantages such as faster etching speeds, greater correctness, and the ability to etch complex designs.
However, it’s necessary to consider the limitations and safety precautions when using these devices. The power output source, operating system/software, battery, cooling system, and connectivity options are critical features of portable laser etchers. Different models and brands have unique features and capabilities, making them suitable for various applications.
Small businesses find handheld laser etchers ideal because they can etch complex designs more precisely and quickly than traditional etchers. To ensure safety, use handheld laser etchers, follow safety instructions, use dry-sprayed metal surfaces, and test the project before etching the main object.
FAQs (Frequently Asked Questions)
1. How strong of a laser do you need to etch metal?
Ans: A laser with a power of at least 30 watts is typically needed to etch metal effectively.
2. How deep is laser etching on metal?
Ans: It can etch metal up to 0.001 inches.
3. Does laser etching wear off?
Ans: Laser etching cannot typically wear off, but it may be possible under specific circumstances.
4. What is laser etching on metal?
Ans: Laser etching on metal is a process that uses a laser to etch or mark designs onto metal surfaces by melting its surface.
5. What kind of laser do you use to etch metal?
Ans: Fiber lasers are commonly used to etch metal due to their high precision and ability to produce fine details.


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The Sacramento Kings take their show on the road beginning their four-game eastern swing Friday night in Brooklyn. They face a disappointing Nets team that has lost five straight and 15-of-17.
Sacramento hasn’t fared much better of late. Losers of five of six, the Kings are struggling to keep up in the race for the eight spot in the Western Conference. The Kings currently sit 2.5 games behind the Utah Jazz for eighth and the Portland Trail Blazers are up on them by two games for the ninth best record in the conference.
Since relieving Lionel Hollins of his head coaching duties last month, Brooklyn is just 2-11 under interim head coach Tony Brown. Rumors of potential trades and/or player buyouts are already surfacing as the Nets slide towards the bottom of the Eastern Conference standings.
Kings by 5.5
WHERE THEY STAND
Kings: 21-28, third place in Pacific
Nets: 12-38, third place in Pacific
MATCHUP TO WATCH
DeMarcus Cousins vs. Brook Lopez -- Lopez is a gifted offensive player that has hurt the Kings in the past. He is just the sort of ground-based big that gives Cousins problems. The Kings All-Star comes into the night nursing an ankle, two knees and a shoulder. He is scheduled to play, but there are no promises on how effective he will be.
Kings: C DeMarcus Cousins (ankle, knees, shoulder) probable, PG Rajon Rondo (turf toe) probable, SG Ben McLemore (wrist) probable, F Eric Moreland (foot) out.
Nets: PG Jarrett Jack (knee) out, G/F Rondae Hollis-Jefferson (ankle) out, F Chris McCullough (knee) out.
The Kings squeaked out a 111-109 victory over the Nets at Sleep Train Arena in mid-November. Sacramento carries a 46-36 all-time franchise lead into Friday night’s contest, but trail the Nets 30-28 in the Sacramento-era.


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United States: Gustavo Arnal, the Chief Financial Officer of famous US retail brand Bed Bath & Beyond plunged to death from the iconic ‘Jenga’ skyscraper located in New York’s Manhattan area.
A man was reported to have jumped from the 18th floor of the skyscraper located at 56 Leonard Street in the Tribeca neighborhood of Manhattan on Friday. He has now been identified as the 52-year-old executive, as per multiple media reports.
Arnal, who was also an executive vice president for the ailing home goods brand jumped from the 60-story building popular for resembling the popular game Jenga due to its misaligned apartment floors atop each other.
Bed Bath & Beyond has been struggling financially and Arnal had reportedly sold 42,513 shares in the company for a little over a $1 million on August 16. The deceased CFO joined the company in 2020 amid the Covid-19 pandemic. Arnal had previously worked for cosmetics giant Avon as a CFO and has had a long stint with Procter & Gamble.
Arnal reportedly earned over $2.9 million via Bed Bath & Beyond in 2021. This included $775,000 in salary and the rest in stock awards. The company had recently announced restructuring which included layoffs and store closures. The move had prompted the Bed Bath & Beyond stock value to slide by a quarter of the value.
READ | Cyrus Mistry, business tycoon and former Tata Sons chairman, this in car crash

domain: economics


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ACF Technology Avoids Unwanted Salt Formation or Corrosion
There are many industrial processes where the prevention of fouling and corrosion caused by hydrochloric acid or ammonium salts is of great importance. Corrosion is a major problem in distillation equipment of oil refineries, petrochemical plants and industrial processes with high acid loads. In oil refineries, corrosion damage is caused or at least greatly accelerated by hydrochloric acid or under-deposit corrosion of ammonium salts.
Although crude oils delivered from production fields are desalted, a small portion of water and salt always remains in the crudes. Sodium, calcium, and magnesium chlorides and sulfates can have detrimental and costly effects on corrosion of oil processing equipment. Common problems are corrosion, erosion or sedimentation of salts in product lines, furnace tubes, pumps, valves and impaired heat transfer due to salt deposits in heat exchangers. Loss of heat-transfer by deposits of salts and corrosion products causes higher energy costs, which contribute negatively to higher CO2 emissions and increase in greenhouse gases.
To prevent salt formation, the operating temperature should be above the sublimation temperature. Unfortunately, this cannot always be achieved or controlled in practice. Ammonium salts are very corrosive to most metals if the salts themselves are wet. White, thick ammonium salt layers often indicate fouling and severe corrosion problems.
Ammonium salt fouling
Many refiners reduce the top temperature of the crude distillation column or FCC main fractionator column. Besides several benefits, reducing the top temperature also bears some risks. Depending on the concentration of certain components in the liquid going up to the top of the column, a lower temperature on the column top trays may lead to deposition of solids like ammonium salts or to development of free water. The formation of salts can cause severe fouling and plugging of valves, loss of separation efficiency, and problems with product quality, increased pressure drop, energy losses and ultimately an unreliable operation of the column. In most cases the only salt deposit mitigation strategy is to implement regular water wash of the column top section which will cause a reduction in unit throughput. Neutralising amines are used as corrosion inhibitors to prevent or at least slow down corrosion. However, the neutralising amine salts formed from the reaction with acidic components are usually also corrosive themselves and can cause damage if they are not removed.
Kurita's ACF Technology is a very effective way to prevent such situations of corrosion or formation of ammonium salt deposits. ACF products are formulations of a very strong organic base. The organic base ACF provides the full base strength of the hydroxide ion. They are about 10 - 100 times stronger than typical organic neutralising amines. This opens up the possibility of both dissolving ammonium salt deposits and, at the same time, also dissolving and removing unwanted deposits of precipitated neutralising amine salts.
ACF completely avoids the negative consequences of inorganic cations like sodium and potassium that would be introduced with caustic solutions. According to the chemical laws of nature, the strong base ACF displaces the weaker base ammonium (NH3) from its salts. ACF salts have a very low corrosion potential with a neutral pH of 7. The formed liquid salts absorb humidity and have a high tendency to stay in the water phase without precipitation. Although ammonium salts dissolve very well in water, a pure water wash does not always have the expected success in practice. The combination of ACF together with washing water often shows significantly better results that cannot be achieved with a pure water wash.
The ACF base has been referred to as a vitamin, although from a classical standpoint it is not. ACF is not known to function as cofactor in any enzymatic reaction. But like vitamins the ACF base plays a significant role in nutrition. The ACF chlorides formed also have no negative influence on the downstream treatment of the wastewater.


Those who oppose bringing in carbon taxes or other emissions-reducing climate policies in Canada frequently argue that there is no need to do so, because Canada’s forests and soil are carbon sinks that already store huge amounts of carbon dioxide (CO2). For example, during the 2017 Conservative Party leadership race, candidate Kevin O’Leary said in an interview, “We have 1.2 billion acres of forest land, we absorb four times more carbon than we emit. We are so lucky that we have this environment that does an incredible job of absorbing so much carbon we do not need to tax ourselves this way.”
Similarly, former Saskatchewan and Manitoba public servant Larry Martin wrote in a 2016 editorial that, based on Canada’s land mass and carbon absorption capacity, “Canada could already be absorbing 20 to 30 percent more CO2 than we emit.” Martin contended that Canada should argue for the inclusion of carbon offset accounting — a way of giving countries credit for natural or constructed carbon storage — under international climate change protocols, saying that Canada could gain as much as $10 billion a year by selling carbon credits to other nations.
But these optimistic scenarios of Canada’s carbon sequestration capacity do not withstand careful scrutiny. While Canada does have 347 million hectares of forest (just under 900 million acres), and while each hectare of mature forest can absorb about 6 tonnes of CO2 per year, unfortunately forests do not just store carbon — they also release it. Every year, millions of tonnes of CO2 is emitted as trees die and decompose, are disturbed by insects like the mountain pine beetle or are burned in forest fires. Fires in the boreal forest, for example, release about 170 tonnes of carbon dioxide per hectare burned. O’Leary’s numbers evidently don’t take carbon emissions from forests into account, while Martin’s numbers are based on a raw estimate of land mass, not a careful assessment of the relative contributions of forests, peatlands and farmlands.
Federal and provincial governments and independent scientists have carefully tracked and estimated carbon storage and emissions levels related to forestry and land use over the years, trying to determine if Canada’s forests, wetlands and farm soils are a net source or a sink of the world’s carbon. And in fact, natural and artificial carbon offsets are already part of our carbon reporting. Every year, Canada submits an estimate of carbon emissions and removals in the National Inventory Report to the United Nations Framework Convention on Climate Change (UNFCCC) — the international carbon reporting framework underlying the Kyoto and Paris agreements. The results have varied widely from year to year, depending on the level of forest fire or insect activity and forestry practices. Canada’s forests have fluctuated from being a net sink of 115 million tonnes of carbon in 1992 to a net source of 221 million tonnes of emissions in 2015, with a wide range of results in years in between.
Under the UNFCCC reporting conventions, countries have a number of options for reporting land use, land-use change and forestry (LULUCF) emissions. The system ensures that there is reasonable consistency in the way countries report their numbers and that countries are primarily held accountable for their human-caused emissions, not the vagaries of forest fires or insect infestations. Canada’s reported emissions, for instance, could spike wildly in a year with heavy forest fire activity.
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Canada has naturally chosen the most favourable reporting options in its national reports. So far this has usually meant excluding LULUCF emissions altogether, since in most years they would have been a net source of emissions. But both the Harper and Trudeau governments signalled their intention to include LULUCF reporting to help meet Canada’s Paris Agreement targets. We are currently projected to fall 232 megatonnes short in 2030. By switching to one of the alternative accounting methodologies for emissions from land use, forestry and forest products allowed under the framework, Canada could narrow the gap — perhaps by as much as 63 or 126 megatonnes — even if our actual emissions don’t change. Canada is also involved in negotiating to allow for carbon credits from one country to be sold to another through what the Paris Agreement calls ITMOs (internationally transferred mitigation outcomes), along the lines Larry Martin was suggesting. But we must remember that any carbon reduction we sell internationally can no longer be counted as a reduction in Canada — it will count in the country that purchases it.
While changing our system of carbon accounting to include natural carbon sinks could bring Canada somewhat closer to meeting our Paris targets, it would be far from a magic bullet. When the effects of natural carbon emissions and events like forest fires are accounted for, Canada’s forests still do not sequester four times more carbon than Canada emits, nor does our land store 20 to 30 percent more carbon than we emit. Canada should certainly continue to pursue improved forestry and farming practices and preservation of our natural wetlands as means of increasing carbon storage, but we cannot claim that these carbon sinks eliminate the need to reduce our fossil fuel use and industrial emissions. To have any hope of meeting our Paris climate commitments, we will need to do both.
Do you have something to say about the article you just read? Be part of the Policy Options discussion, and send in your own submission. Here is a link on how to do it. | Souhaitez-vous réagir à cet article ? Joignez-vous aux débats d’Options politiques et soumettez-nous votre texte en suivant ces directives.


text:
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from Jellyoasis Inc., originally released 12th September, 2012
Be the Lich king and manage your deadly towers and cast devastating magic in this incredibly addictive real-time strategy tower type defense game!
Decimate and annihilate invaders in new and exciting ways each level....
Recent posts about Lich Defense

domain: entertainment


Issue No. 03 - March (1988 vol. 14)
DOI Bookmark: http://doi.ieeecomputersociety.org/10.1109/32.4650

The RTAG (real-time asynchronous grammars) programming language is discussed. The language is based on an attribute grammar notation for specifying protocols. Its main design goals are: (1) to support concise and easily understood expression of complex real-world protocols; and (2) to serve as the basis of a portable software system for automated protocol implementation. The algorithms used in generating implementations from given specifications are sketched, and a Unix-based automated implementation system for RTAG is described.

automated protocol implementation; RTAG; real-time asynchronous grammars; programming language; attribute grammar notation; portable software system; Unix-based automated implementation; grammars; protocols
D. Anderson, "Automated Protocol Implementation with RTAG," in IEEE Transactions on Software Engineering, vol. 14, no. , pp. 291-300, 1988.


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Escape the fast-paced lifestyle for a week, and treat yourself to a much-needed getaway. If you’re getting bogged down by work and other daily stresses, you probably need a bit of beach therapy. Get your fix of vitamin sea and make the trip from Philadelphia to Outer Banks.
Before you hit the road, plan your week with our free Outer Banks Vacation Guide. Find the coolest restaurants, outdoor adventures, and lively entertainment on the barrier islands of North Carolina!
Why You Should Make the Trip From Philadelphia to Outer Banks
You Need to Escape Daily Stresses of Living in a Busy City
If you’re feeling burned out from everything going on in your life, it’s time to step back for a moment and enjoy the sunshine. Traveling, in general, is a known way to relieve stress, and traveling to the Outer Banks is sure to put a smile on your face!
Outer Banks Food is Phenomenal
Locally-sourced dishes aren’t difficult to find along these North Carolina shores. Select from a wide variety of local seafood restaurants, southern-style barbeque, and more. We could go on and on about the amazing restaurants spread throughout town, but a few that we recommend are Mike Dianna’s Grill Room in Corolla, The Blue Point in Duck, and Coastal Provisions in Southern Shores.
There Are Numerous Ways to Bask in the Sunshine
Dip your paddle into the peaceful Currituck Sound and kayak through the serene OBX waters. Looking for more of a thrill? Soar through the air as the waves crash beneath you, and go parasailing with North Beach Watersports! They also offer jet skis, tubes, standup paddleboards, kayaks, and pontoons!
Our Coast is Rich With History
Use this getaway as an opportunity to learn new things! There are tons of important events in history that have made the Outer Banks famous. Sure, Philly is known for its extensive history, but the OBX coast also had a prominent role in the making of our nation!
You can visit the spot where the first flight took off, or step onto the boat that carried the first English colonists to the New World, the Elizabeth II in Manteo. Why read about it in textbooks or on the internet when you can see it for yourself?
You Can Make the Road Trip Almost As Fun as the Vacation Itself!
The driving distance from Philly to the Outer Banks is around 350 miles if you take US-13 S. If seven hours of driving doesn’t seem appealing to you, try splitting the road trip up by stopping at cool attractions along the way! Plus, the Outer Banks is so worth it!
Here are some popular destinations you should check out when it’s time to stretch your legs!
- Chesapeake Bay Bridge-Tunnel (It’s an excellent spot for birding!)
- Virginia Beach, Virginia
- Williamsburg, Virginia
You’ve Arrived in the Outer Banks!
Unpack your bags in a luxury Outer Banks vacation rental. The best way to relax after a day of driving is by spending an evening on a private deck accompanied by gentle sounds of the ocean. You can do this in our Paramount Destinations vacation rentals!
Reserve our Memories vacation home in Corolla for peaceful sunrises on the deck and afternoons in the private saltwater pool.
So, what are you waiting for? Your relaxing escape awaits on the Outer Banks. Check our availability and book your getaway today!

domain: geography